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EFFECTS OF BIOREACTOR OPERATION PARAMETERS ON INTRACELLULAR REACTION RATE DISTRIBUTION IN BETA-LACTAMASE PRODUCTION BY Bacillus SPECIES
A THESIS SUBMITTED TO THE GRADUATE SCHOOL OF NATURAL AND APPLIED SCIENCES
OF THE MIDDLE EAST TECHNICAL UNIVERSITY
BY
MÜGE ARİFOĞLU
IN PARTIAL FULFILLMENT OF THE REQUIREMENTS FOR
THE DEGREE OF MASTER OF SCIENCE IN
CHEMICAL ENGINEERING
AUGUST 2004
Approval of the Graduate School of Natural and Applied Sciences
Prof. Dr. Canan Özgen
Director
I certify that this thesis satisfies all the requirements as a thesis for the degree of Master of Science.
Prof. Dr. Timur Doğu Head of Department
This is to certify that we have read this thesis and that in our opinion it is fully adequate, in scope and quality, as a thesis and for the degree of Master of Science.
Prof. Dr. Güzide Çalık Co-Supervisor
Assoc. Prof. Dr. Pınar Çalık
Supervisor
Examining Committee Members
Prof. Dr. Türker Gürkan (METU, CHE)
Assoc. Prof. Dr. Pınar Çalık (METU, CHE)
Prof. Dr. Güzide Çalık (Ankara Univ., CHE)
Prof. Dr. H. Tunçer Özdamar (Ankara Univ., CHE)
Assoc. Prof. Dr. Nihal Aydoğan (Hacettepe Univ., CHE)
iii
I hereby declare that all information in this document has been obtained and presented in accordance with academic rules and ethical conduct. I also declare that, as required by these rules and conduct, I have fully cited and referenced all material and results that are not original to this work. Name, Last name : Müge Arifoğlu
Signature :
iv
ABSTRACT
EFFECTS OF BIOREACTOR OPERATION PARAMETERS ON
INTRACELLULAR REACTION RATE DISTRIBUTION IN
BETA-LACTAMASE PRODUCTION BY Bacillus SPECIES
Arifoğlu, Müge
M.S., Department of Chemical Engineering
Supervisor: Assoc. Dr. Pınar Çalık
Co-Supervisor: Prof. Dr. Güzide Çalık
August 2004, 120 pages
In this study, the effects of oxygen transfer (OT) on β-lactamase
production and on intracellular reaction rates were investigated with Bacillus
licheniformis ATCC 2597. In order to clarify the oxygen transfer effects on the
production of β-lactamase, firstly a glucose based defined medium was designed
and using this medium, the effects of bioreactor operation parameters, i.e., pH
and temperature, on β-lactamase activity and cell formation were investigated in
laboratory scale batch-bioreactors using shake bioreactors having V=33 ml
working volumes. Among the investigated bioprocess conditions, the highest β-
lactamase activity was obtained as A=115 U cm-3, in the medium with 7.0 kg m-3
glucose, 7.1 kg m-3 (NH4)2HPO4 and the salt solution, at pH0=7.5, T=37°C,
N=200 min-1. At the optimum conditions found in laboratory scale the effects of
OT on cell generation, substrate consumption, product (β-lactamase) and by-
products formations were investigated at three different air inlet (Q0/ VR = 0.2,
0.5 and 1 vvm) and at three agitation rates (N=250, 500, 750 min-1) in V = 3.0
dm3 batch bioreactors consisting of temperature, pH, foam, stirring rate and
dissolved oxygen controls. Along with the fermentation, cell, substrate and by-
product concentrations, β-lactamase activity, yield coefficients, specific rates,
v
oxygen uptake rates and the liquid phase mass transfer coefficient values were
determined. The highest β-lactamase activity was obtained at 0.5 vvm 500 min-1
and at 0.2 vvm 500 min-1 conditions as ca. A=90 U cm-3 while the highest cell
concentration was obtained as Cx=0.67 kg m-3 at 0.5 vvm 750 min-1 and at 0.2
vvm 750 min-1 conditions. KLa, increased with the increase in the agitation and
aeration rates and its values varied between 0.007-0.044 s-1 and oxygen uptake
rate varied between 0.4-1.6 mol m-3 s-1. Finally, the influence of OT conditions on
the intracellular reaction rates was investigated using metabolic flux analysis to
evaluate the effects of oxygen on the metabolism.
Keywords: β-lactamase, production, Bacillus, oxygen transfer, metabolic flux
analysis
vi
ÖZ
Bacillus TÜRLERİ İLE BETA-LAKTAMAZ ÜRETİMİNDE
BİYOREAKTÖR İŞLETİM PARAMETRELERİNİN HÜCRE İÇİ
TEPKİME HIZ DAĞILIMLARINA ETKİLERİ
Arifoğlu, Müge
Yüksek Lisans, Kimya Mühendisliği Bölümü
Tez Yöneticisi: Doç. Dr. Pınar Çalık
Ortak Tez Yöneticisi: Prof. Dr. Güzide Çalık
Ağustos 2004, 120 sayfa
Bu çalışmada, Bacillus licheniformis ATCC 25972 ile oksijen aktarımının β-
laktamaz üretimine ve hücreiçi tepkime hızlarına etkisi araştırılmıştır. Bu amaçla
önce glukoz temelli tanımlanmış ortam tasarımı yapılmış ve tasarlanan bu üretim
ortamı kullanılarak biyoproses işletim parametrelerinden pH ve sıcaklığın β-
laktamaz üretimine ve hücre oluşumuna etkileri, laboratuvar ölçekli, V=33 ml
çalışma hacımlı kesikli biyoreaktörler kullanılarak araştırılmıştır. En yüksek
aktivite, 7.0 kg m-3 glukoz, 7.1 kg m-3 (NH4)2HPO4, ve tuz çözeltisini içeren
ortamda, pH0=7.5, T=37°C, N=200 dk-1 koşullarında, A=115 U cm-3 olarak
bulunmuştur. Laboratuvar ölçekte bulunan en uygun koşullar kullanılarak,
oksijen aktarımının substrat tüketimine, mikroorganizma derişimine, ürün (β-
laktamaz) ve yan-ürün oluşumuna etkileri üç farklı hava giriş (Q0/ VR = 0.2, 0.5
and 1 vvm) ve karıştırma hızlarında ( N=250, 500, 750 dk-1) V= 3.0 dm3 hacımlı,
sıcaklık, pH, köpük, karıştırma ve çözünmüş oksijen derişimi kontrollü kesikli
biyoreaktörde araştırılmıştır. Proses sürecince, farklı oksijen aktarım koşullarında
hücre, substrat ve yan-ürün derişimleri, β-laktamaz aktivitesi, verim katsayıları,
spesifik hızlar, oksijen tüketim hızları ve sıvı faz kütle aktarım katsayıları (KLa)
bulunmuştur. En yüksek enzim aktivitesine A=90 U cm-3 olarak 0.5 vvm, 500
dk-1 ve 0.2 vvm 500 dk-1 koşullarında ulaşılırken, en yüksek hücre derişimine
vii
Cx=0.67 kg m-3 olarak 0.5 vvm 750 dk-1 ve 0.2 vvm 750 dk-1 koşullarında
ulaşılmıştır. KLa, havalandırma ve karıştırma hızları artıkça artmış ve değeri
0.007-0.044 s-1 aralığında değişmiştir. Oksijen tüketim hızı ise 0.4-1.6 mol m-3 s-1
aralığında değişmiştir. Son olarak B.licheniformis ile β-laktamaz üretiminde oksijen
aktarım koşullarının hücreiçi tepkime hızlarına etkisi metabolik akı analizi ile
bulunmuştur.
Anahtar Kelimeler: β-laktamaz, üretim, Bacillus, oksijen aktarımı, metabolik
akı analizi
viii
To My Family
ix
ACKNOWLEDGEMENTS
I wish to express my sincere gratitude to my supervisor Assoc. Prof. Dr.
Pınar Çalık and my co-supervisor Prof. Dr. Güzide Çalık for their guidance,
advice, criticism, encouragements and insight throughout the research.
I would also like to express my appreciation to Prof. H. Tunçer Özdamar for
giving me every opportunity to use the laboratories in Ankara University. And I
wish to thank all the members of his research group for their guidance, patience
and friendship during the experiments I performed in Ankara University.
I also wish to give my special thanks to all my friends in our research
group in Industrial Biotechnology Laboratory. I am especially grateful to Pınar
Yılgör, Pınar Kocabaş, İlkin Ece Telli, Peruze Ayhan, Eda Çelik and Ceren Oktar
for their valuable help, cooperation and friendship.
Financial Support provided by TUBITAK through project MISAG-258 and
METU-Research Fund are gratefully acknowledged.
Finally, I would like to express my deepest thanks to my family for
supporting, encouraging and loving me all through my life.
x
TABLE OF CONTENTS
PLAGIARISM ........................................................................................... iii
ABSTRACT.............................................................................................. iv
ÖZ......................................................................................................... vi
DEDICATION..........................................................................................viii
ACKNOWLEDGEMENTS ............................................................................. ix
TABLE OF CONTENTS ................................................................................ x
LIST OF TABLES .....................................................................................xiii
LIST OF FIGURES ................................................................................... xv
NOMENCLATURE.................................................................................... xvii
CHAPTER
1. INTRODUCTION.................................................................................... 1
2. LITERATURE SURVEY............................................................................. 5
2.1 Enzymes......................................................................................... 5
2.1.1 General Characteristics.............................................................. 5
2.1.2 Nomenclature and Classification of Enzymes................................. 6
2.1.3 Enzyme Activity........................................................................ 6
2.2 Beta-Lactamases ............................................................................. 7
2.3 Bioprocess Parameters in Enzyme Production ....................................... 9 2.3.1 Microorganism.......................................................................... 9 2.3.1.1 The Genus Bacillus ....................................................... 10 2.3.1.2 Major Metabolic Pathways and Regulations ...................... 10 2.3.1.3 Cell Growth, Kinetics and Yield Factors ............................ 16 2.3.2 Medium Design....................................................................... 20 2.3.3 Bioreactor Operation Parameters .............................................. 22
2.3.3.1 Temperature................................................................ 22
xi
2.3.3.2 pH ............................................................................. 23 2.3.3.3 Oxygen Transfer Rate ................................................... 24
2.4 Metabolic Flux Analysis .................................................................... 33
2.4.1 Modelling of Bioreaction Network for Metabolic Flux Analysis ......... 34 2.4.2 Solution of Mathematical Model................................................. 35
3. MATERIALS AND METHODS .................................................................. 38
3.1 Chemicals ..................................................................................... 38
3.2 The Microorganism ......................................................................... 38
3.3 The Solid Medium........................................................................... 38
3.4 The Precultivation Medium............................................................... 39
3.5 The Production Medium................................................................... 39
3.6 Analysis........................................................................................ 40 3.6.1 Cell Concentration .................................................................. 41 3.6.2 Beta-Lactamase Activity .......................................................... 41 3.6.3 Beta-Lactamase and Serine Alkaline Protease Concentrations........ 41 3.6.4 Reduced Sugar Concentration................................................... 41 3.6.5 Amino Acid Concentrations....................................................... 42 3.6.6 Organic Acid Concentrations..................................................... 42 3.6.7 Liquid Phase Mass Transfer Coefficient and Oxygen Uptake Rate.... 43
3.7 Mass Flux Balance-Based Analysis .................................................... 43
4. RESULTS AND DISCUSSION ................................................................. 44
4.1 Medium Design .............................................................................. 44 4.1.1 Effect of Nitrogen Source Concentration ..................................... 44
4.2 Bioreactor Operation Parameters ...................................................... 45 4.2.1 Effect of pH and Temperature................................................... 46 4.2.2 Effect of Carbon Source Concentration ....................................... 47 4.2.3 The Optimized Medium ............................................................ 48
4.3 Effect of Oxygen Transfer ................................................................ 48 4.3.1 Dissolved Oxygen Concentration and pH Profiles ......................... 49 4.3.2 Glucose Concentration Profiles.................................................. 51 4.3.3 Cell Concentration Profiles ....................................................... 52
4.3.4 Beta-Lactamase Activity Profiles ............................................... 53
xii
4.3.5 Amino Acid Concentrations....................................................... 54 4.3.6 Organic Acid Concentrations..................................................... 59 4.3.7 Oxygen Transfer Characteristics................................................ 62 4.3.7.1 Volumetric Oxygen Transfer Coefficient ........................... 63 4.3.7.2 Oxygen Uptake Rate ..................................................... 65 4.3.8 Specific Growth Rates and Yield Coefficients ............................... 69
4.4 Metabolic Flux Analysis ................................................................... 74
4.4.1 Metabolic Flux Analysis for LimOT condition ................................ 76 4.4.2 Metabolic Flux Analysis for LOT1 condition .................................. 78 4.4.3 Metabolic Flux Analysis for MOT1 condition ................................. 80 4.4.4 Metabolic Flux Analysis for HOT2 condition.................................. 81
5. CONCLUSION ..................................................................................... 95
REFERENCES ....................................................................................... 103
APPENDICES........................................................................................ 109
A. Calibration of Bacillus licheniformis Concentration.................................. 109
B. Calibration of Beta-Lactamase Activity ................................................. 110
C. Calibration of Beta-lactamase Concentration......................................... 111
D. Calibration of Serine Alkaline Concentration.......................................... 112
E. Preparation of DNS Solution ............................................................... 113
F. Calibration of Reduced Sugar Concentration.......................................... 114
G. Metabolic Reactions for Bacillus licheniformis ........................................ 115
xiii
LIST OF TABLES
TABLE
2.1 International classification of enzymes ................................................... 7
2.2 Summary of batch cell growth............................................................. 17
2.3 Definition of yield coefficients.............................................................. 19
2.4 The major macronutrient elements, their physiological functions, growth
requirements and common sources................................................... 21
2.5 Parameter values for the emprical correlation of KLa............................... 29
3.1 The composition of the solid medium for Bacillus sp. .............................. 38
3.2 The composition of the precultivation medium....................................... 39
3.3 The composition of the reference production medium ............................. 40
4.1 Oxygen transfer conditions ................................................................. 49
4.2.a The variations in amino acid concentrations in the fermentation broth
with the cultivation time at LimOT condition........................................ 56
4.2.b The variations in amino acid concentrations in the fermentation broth
with the cultivation time at LOT1 condition.......................................... 56
4.2.c The variations in amino acid concentrations in the fermentation broth
with the cultivation time at LOT2 condition.......................................... 57
4.2.d The variations in amino acid concentrations in the fermentation broth
with the cultivation time at MOT1 condition ......................................... 57
4.2.e The variations in amino acid concentrations in the fermentation broth
with the cultivation time at MOT2 condition ......................................... 58
4.2.f The variations in amino acid concentrations in the fermentation broth
with the cultivation time at HOT1 condition ......................................... 58
4.2.g The variations in amino acid concentrations in the fermentation broth
with the cultivation time at HOT2 condition ......................................... 59
xiv
4.3. The variations in organic acid concentrations in the fermentation broth
with the cultivation time at LimOT, LOT1, LOT2, MOT1, MOT2, HOT1 and
HOT2 conditions .............................................................................. 60
4.4 The variations of total organic acid concentration and non-excreted
organic acids with the constant air inlet and agitation rate .................... 62
4.5.a The variations in oxygen transfer parameters with cultivation time at
LimOT, LOT1 and LOT2 conditions ...................................................... 66
4.5.b The variations in oxygen transfer parameters with cultivation time at
MOT1, MOT2, HOT1 and HOT2 conditions ............................................. 67
4.6 The variations in oxygen transfer coefficients obtained from different
correlations and the average experimental value ................................. 68
4.7.a The variations in specific rates and yield coefficients with cultivation
time at LimOT, LOT1 and LOT2 conditions ........................................... 72
4.7.b The variations in specific rates and yield coefficients at MOT1, MOT2,
HOT1 and HOT2 conditions................................................................ 73
4.8 Metabolic flux distribution of β-lactamase fermentation of B.licheniformis
at LimOT, LOT1, MOT1 and HOT2 conditions ........................................ 83
4.9 ATP generation throughout the fermentation ......................................... 94
xv
LIST OF FIGURES FIGURE 2.1 Hydrolysis of penicillins and cephalosporins by β-lactamase...................... 8
2.2 Overview of steps in the overall mass transfer of oxygen from a gas
buble to the reaction site inside the individual cells .............................. 25
2.3 Variation of dissolved oxygen concentration with time in dynamic
measurement of KLa. ....................................................................... 31
2.4 Evaluting KLa using the Dynamic Method ............................................. 31
4.1 The variation in β-lactamase activity with initial nitrogen concentration .... 45
4.2 The variations in β-lactamase activity with the initial pH. ....................... 46
4.3 The variations in β-lactamase activity with the initial pH and
temperature of the cultivation medium ............................................... 47
4.4 The variations in β-lactamase activity with the initial glucose
concentration .................................................................................. 48
4.5 The variations in dissolved oxygen concentration with cultivation time ..... 50
4.6 The variations in medium pH with cultivation time ................................ 51
4.7 The variations in glucose concentration with cultivation time .................. 52
4.8 The variations in cell concentration with cultivation time ........................ 53
4.9 The variations in β-lactamase activity with cultivation time..................... 54
4.10 The variations in total organic acid concentration with cultivation time .... 61
4.11 Correlation between the power nmber and the reynold number for a
bioreactor system with one-six bladed Rushton turbine impeller and
baffles........................................................................................... 64
xvi
4.12 The variations in specific growth rate with cultivation time .................... 70
4.13 The variations in specific substrate consumption rate with the cultivation
time .............................................................................................. 70
4.14 The variations in specific oxygen uptake rate with the cultivation time ... 71
4.15 The variations in specific β-lactamase production rate with the cultivation
time .............................................................................................. 71
4.16 The variations of cell and β-lactamase concentrations with the cultivation
time .............................................................................................. 75
4.17 The variations of SAP concentration with the cultivation time ................. 76
xvii
NOMENCLATURE
a The gas liquid interfacial area per unit liquid volume, m2 m-3
A Beta-lactamase activity, U cm-3
Aλ Absorbance
Ae Aeration number (=Q / NDI3 )
c (t) Metabolite accumulation vector
c1 (t) Extracellular metabolite accumulation vectors
c2 (t) Intracellular metabolite accumulation vectors
CAA Amino acid concentration, kg m-3
CB β-lactamase concentration, kg m-3
CC Citric Acid concentration, kg m-3
CG Glucose concentration, kg m-3
CG0 Initial glucose concentration, kg m-3
CN Nitrogen concentration, kg m-3
CN0 Initial nitrogen concentration, kg m-3
COA Organic acid concentration, kg m-3
CO Dissolved oxygen concentration, mol m-3; kg m-3
Co0 Initial dissolved oxygen concentration, mol m-3; kg m-3
CO* Oxygen saturation concentration, mol m-3; kg m-3
CSAP Serine alkaline protease concentration, kg m-3
CX Cell concentration, kg dry cell m-3
Da Damköhler number (=OD / OTRmax; Maximum possible oxygen
utilization rate per maximum mass transfer rate)
D Bioreactor diameter, m
DI Impeller diameter, m
E Enhancement factor (=KLa / KLao); mass transfer coefficient with
chemical reaction per physical mass transfer coefficient
Fr Froude number, (=N2DI/g )
KLa0 Physical overall liquid phase mass transfer coefficient; s-1
KLa Overall liquid phase mass transfer coefficient; s-1
xviii
N Agitation or shaking rate, min–1
Np Power number
P Power input in gas-free stirred liquid, W
PG Power input in aerated stirred liquid, W
pH0 Initial pH
Qo Volumetric air feed rate, m3 min-1
qo Specific oxygen uptake rate, kg kg –1 DW h-1
qs Specific substrate consumption rate, kg kg –1 DW h-1
r Volumetric rate of reaction, mol m-3 s-1
r(t) Vector of reaction fluxes
Re Reynolds number, (=NDI2ρ/µ )
r0 Oxygen uptake rate, mol m-3 s-1; kg m-3 h-1
rP Product formation rate, kg m-3 h-1
rS Substrate consumption rate, kg m-3 h-1
rX Rate of cell growth, kg m-3 h-1
t Bioreactor cultivation time, h
T Bioreaction medium temperature, °C
TAA Total amino acid concentration, kg m-3
TOA Total organic acid concentration, kg m-3
U One unit of an enzyme
V Volume of the bioreactor, m3
VR Volume of the bioreaction medium, m3
VS Superficial gas velocity, m s-1
YX/S Yield of cell on substrate, kg kg-1
YX/O Yield of cell on oxygen, kg kg-1
YS/O Yield of substrate on oxygen, kg kg-1
YP/X Yield of product on cell, kg kg-1
YP/S Yield of product on substrate, kg kg-1
YP/O Yield of product on oxygen, kg kg-1
Z Objective function
Greek Letters
η Effectiveness factor (=OUR/OD; the oxygen uptake rate per
maximum possible oxygen utilization rate)
µ Specific cell growth rate, h-1
µ max Maximum specific cell growth rate, h-1
xix
λ Wavelength, nm
αi Stoichiometric coefficient of the fluxes
ρl Liquid phase density, kg m-3
Abbreviations
Ac Acetic acid
AcCoA Acetyl coenzyme A
ADEPT Antibody-Directed Enzyme Prodrug Therapy
ADP Adenosine 5’-diphosphate
ADPHep ADP-D-glycerol-D-mannoheptose
Ala Alanine
AMP Adenosine 5’-monophosphate
Arg Arginine
Asn Asparagine
Asp Aspartic acid
AspSa Aspartate semialdehyde
ATP Adenosine 5’-triphosphate
ATCC American Type Culture Collection
But Butyric acid
C14:0 Myristic acid
C14:1 Hydroxymyristic acid
CaP Carbamoyl-phosphate
CDP Cytidine 5’-diphosphate
CDPEtN CDP-ethanolamine
Cit Citrate
Citr Citruline
Chor Chorismate
CMP Cytidine 5’-monophosphate
CMPKDO CMP-3-deoxy-D-manno-octulosonic acid
CO2 Carbondioxide
CTP Cytidine 5’-triphosphate
Cys Cysteine
dATP 2’-Deoxy-ATP
dCTP 2’-Deoxy-CTP
dGTP 2’-Deoxy-GTP
dTTP 2’-Deoxy-TTP
xx
DC L-2,3 dihyrodipicolinate
DHF 7,8-Dihydrofolate
DNS Dinitrosalisylic acid
DO Dissolved oxygen
E4P Erythrose 4-phosphate
EC Enzyme Commission
F10THF N10-Formyl-THF
F6P Fructose 6-phosphate
FA Fatty acids
FADH Flavine adeninedinucleotide (reduced)
Frc Fructose
Fum Fumarate
G1P Glucose 1-phosphate
G6P Glucose 6-phosphate
GDP Guanosine 5’-diphosphate
GL3P Glycerol 3-phosphate
Glc Glucose
Gln Glutamine
Glu Glutamate
Gluc Gluconate
Gluc6P Gluconate 6-phosphate
Glx Glyoxylate
Gly Glycine
GMP Guanosine 5’-monophosphate
GTP Guanosine 5’-triphosphate
H2S Hydrogen sulfide
His Histidine
HOT1 High-oxygen transfer (Q0/VR = 1.0 vvm, N =500 min-1 condition)
HOT2 High-oxygen transfer (Q0/VR = 0.5 vvm, N =750 min-1 condition)
HSer Homoserine
ICit Isocitrate
IGP Indoleglycerolphosphate
Ile Isoleucine
IMP Inosinemonophosphate
αKG α-ketoglutarate
Kval Ketovaline
Lac Lactate
xxi
Leu Leucine
LimOT Limited-oxygen transfer (Q0/VR =0.2 vvm, N =250 min-1 condition)
LOT1 Low-oxygen transfer (Q0/VR = 0.5 vvm, N =250 min-1 condition)
LOT2 Low-oxygen transfer (Q0/VR = 0.2 vvm, N =500 min-1 condition)
Lys Lysine
Mal Malate
Man Mannose
Man6P Mannose 6-phosphate
mDAP meso-Diaminopimelate
Met Methionine
MeTHF N5- N10-methenyl-THF
MetTHF N5- N10-methylene-THF
MFA Metabolic Flux Analysis
MOT1 Medium-oxygen transfer (Q0/VR=0.5 vvm, N=500 min-1 condition)
MOT2 Medium-oxygen transfer (Q0/VR=0.2 vvm, N=750 min-1 condition)
MTHF N5- methyl-THF
NADH Nicotinamide-adeninedinucleotide (reduced)
NADPH Nicotinamide-adeninedinucleotide phosphate (reduced)
NH3 Ammonia
OA Oxaloacetic acid
Orn Ornithine
OD Oxygen demand (=µmax CX / YX/O; mol m-3 s-1)
OUR Oxygen uptake rate, mol m-3 s-1
OTR Oxygen transfer rate, mol m-3 s-1
OTRmax Maximum possible mass transfer rate (=KLaCO*; mol m-3 s-1)
PEP Phosphoenolpyruvate
PG3 Glycerate 3-phosphate
Phe Phenylalanine
Pi Inorganic ortophosphate
PPi Inorganic pyrophosphate
PRAIC 5’-Phosphoribosyl-4-carboxamide-5-aminoimidazole
Pro Proline
PRPP 5-Phospho-D-ribosylpyrophosphate
Pyr Pyruvate
R5P Ribulose 5-phosphate
Rib5P Ribose 5-phosphate
RPM Reference production medium
xxii
S7P Sedoheptulose-7-phosphate
SAP Serine Alkaline Protease
Ser Serine
Suc Succinate
SucCoA Succinate coenzyme A
Xyl5P Xylulose 5-phosphate
TCA Tricarboxylic acid
Tet L-2,3,4,5 Tetrahydrodipicolinate
T3P Triose 3-phosphate
THF Tetrahydrofolate
Thr Threonine
Trp Tyrptophan
Tyr Tyrosine
UDP Uridine 5’-diphosphate
UDPGlc UDP-glucose
UDPNAG UDP-N-Acetyl-glucosamine
UDPNAM UDP-N-Acetyl-muramic acid
UMP Uridine 5’-monophosphate
UTP Uridine 5’-triphosphate
Val Valine
1
CHAPTER 1
INTRODUCTION
Biotechnology is the integrated use of natural sciences (biology,
biochemistry, molecular biology, chemistry and physics) and engineering
sciences (chemical reaction engineering, electronics) to the processing of
materials by biological agents to provide goods and services (Moser, 1988).
Biotechnology has produced new products and processes in a number of
economic sectors including agriculture, food processing, chemical and
pharmaceutical industries, pesticides, detergents, feed stocks, recycling, and
waste treatment.
Enzymes are one of the most important products of biotechnological
processes. Industrial biotechnology companies develop new enzymes,
biocatalysts, to be used in manufacturing processes of other industries.
Enzymes are proteins produced by all living organisms. They are characterized
according to the compounds they act upon.
Industrial biotechnology companies look for biocatalysts with industrial
value in the natural environment; improve the biocatalysts to meet very specific
needs and manufacture them in commercial quantities using fermentation
systems. In some cases, genetically altered microbes (bacteria, yeast, etc.), in
others, naturally occurring microbes carry out the fermentation.
Some industrial enzymes are extracted from animal or plant tissues. Plant
derived commercial enzymes include proteolytic enzymes papain, bromelain and
ficin and some other specialty enzymes like lipoxygenase from soybeans. Animal
derived enzymes include proteinases like pepsin and rennin (Leisola et al.,
2001). Most of the enzymes are, however, produced by microorganisms in
submerged cultures. The use of microorganisms as a source material for enzyme
production has developed for several important reasons. These are the:
• Short operation time,
2
• Cheap production medium,
• High specific activity per unit dry weight of product,
• Nonoccurrence of seasonal fluctuations of raw materials and possible
shortages due to climatic changes or political upheaval (Goel et al.,
1994),
• Availability of a wide spectrum of enzyme characteristics, such as pH
range and temperature resistance for selection,
• Possibility of increasing enzyme production by modifying the medium
composition or by genetic manipulation of the microorganism.
Presently the industrial enzyme companies sell enzymes for a wide variety
of applications. Detergents, textiles, starch, baking, animal feed, and
pharmaceuticals are the main industries using these industrially produced
enzymes. The estimated value of world enzyme market was about US $ 1.3
billion in 2000 and it has been forecasted to grow to almost US $ 2 billion by
2005 (Leisola et al., 2001).
β-lactamases, which are one of the most important industrial enzymes,
catalyze the hydrolysis of the β-lactam ring in the β-lactam antibiotics, i.e.,
penicillins and cephalosporins and antibiotically inactive products are formed.
Actually β-lactamases are the primary agents of bacterial resistance to
antibiotics. They are manufactured for the specific assay of penicillins,
destruction of residual penicillins / cephalosporins in body fluids and culture
media, sterility tests of penicillins, treatment of penicillin sensitivity reactions,
penicillin electrodes and for drug design (White and White, 1997). Recently, the
development of β-lactamase dependent prodrugs with the applications in
antibody-directed enzyme prodrug therapy (ADEPT) has been an area of
particular interest (Tang et al., 2003).
In enzyme production by bioprocesses, there are some important factors
that must be taken into account in order to get high yield, selectivity and
productivity. These are the microorganism, medium design and bioreactor
operation conditions, i.e., oxygen transfer rate, pH and temperature.
3
Selection of a proper microorganism is very important in bioprocesses since
microorganisms act as microbioreactors in the bioreactor operation systems.
Therefore the microorganisms used should be stable, should not produce toxins
and its enzyme production capacity should be high. Beta-lactamases, like most
of the commercial enzymes, are industrially produced mostly by Bacillus species
due to their ability to secrete high amounts of extracellular enzymes.
In bioprocesses besides the selection of the most potential producer, the
medium composition is indeed important. Carbon and energy sources and their
concentrations are important as they are the tools for bioprocess medium design
(Çalık et al., 2001).
Oxygen transfer, pH, and temperature that are the major bioreactor
operation conditions show diverse effects on product formation in aerobic
fermentation processes by influencing metabolic pathways and changing
metabolic fluxes (Çalık et al., 1999). In general, according to cell growth
conditions and metabolic pathway analysis, some bioprocesses require high
oxygen transfer rate conditions, while others require controlled oxygen transfer
rates in order to regulate oxygen uptake rates (Çalık et al., 1998).
In Bacillus, substrate and medium design, and bioreactor operation
conditions, e.g. oxygen transfer rate and pH, regulate enzyme formation
throughout the bioprocess. In this context, the regulation of the intracellular
reaction network towards the synthesis of the desired enzyme in a well designed
medium is indeed important in order to increase the yield and selectivity within
the ultimate limit of the production capacity of the cell (Çalık et al., 2001).
Because metabolic reactions are intimately coupled with bioreactor-
operation conditions, metabolic flux analysis, in addition to the successful
application of metabolic engineering, is helpful in describing the interactions
between the cell and the bioreactor for the purpose of fine tuning the bioreactor
performance. Therefore, knowing the distribution of the metabolic fluxes during
the growth, product, and by-product formations in the bioreactor provides new
information for understanding physiological characteristics of the microorganism
and reveals important features of the regulation of the bioprocess for enzyme
production (Çalık et al., 1998).
4
Because of the medical implications of β-lactamase, it has been focus of
intense research over the last half century, however, mostly from the point of
view of enzyme induction, secretion and purification.
Related with medium design, the effect of glucose was investigated for
improving β-lactamase production (Hemila et al., 1992). Among the bioreactor
operation parameters, the effects of pH (Sargent et al., 1968; Hemila et al.,
1992), temperature (Bernstein et al., 1967; Kuennen et al.,1980; Hemila et al.,
1992) and dissolved oxygen (Sargantanis and Karim, 1996; 1998) on β-
lactamase production are reported (Çelik, 2003). In the recent study of Çelik and
Çalık (2004) bioprocess design parameters for β-lactamase production by
Bacillus species were investigated. However in the literature there are no studies
related with the metabolic flux analysis for β-lactamase production and the
influence of oxygen-transfer conditions on the intracellular metabolic flux
distributions.
In this study, the defined medium was designed in terms of its carbon and
nitrogen sources concentration. Thereafter, by using the designed medium, the
effects of bioprocess operation parameters, i.e., pH and temperature, on β-
lactamase activity were investigated in laboratory scale bioreactors. Then, using
the optimum bioprocess parameters, the effects of oxygen transfer on the β-
lactamase production and variations in the by-product concentration were
investigated. Finally, metabolic flux analysis for β-lactamase production was
made and the influence of oxygen transfer conditions on the intracellular
metabolic flux distributions in B.licheniformis under well-defined batch bioreactor
conditions was investigated to evaluate the effects on the metabolism of the
bacilli in the β-lactamase fermentation process.
5
CHAPTER 2
LITERATURE SURVEY
2.1 Enzymes
2.1.1 General Characteristics
Enzymes are usually proteins of high molecular weight (15,000 < MW<
several million daltons) that act as catalysts. Some RNA molecules are also
catalytic, but the vast majority of cellular reactions are mediated by protein
catalysts (Shuler and Kargi, 1992).
Similar to chemical catalyst, enzymes lower the activation energy of the
reaction catalyzed without undergoing a permanent chemical change. While a
catalyst influences the rate of a chemical reaction, it does not affect reaction
equilibrium. Catalytic activity of enzymes differs from that of other catalysts as
follows:
1) Enzymes are highly efficient, with turnover numbers (N, i.e. the number
of molecules associated with a site per second) frequently higher than those of
inorganic catalysts, especially when considering reactions carried out within the
physiological temperature range 25-37°C.
2) Enzyme reactions are specific in the nature of the reaction catalyzed and
the substrate utilized.
3) Enzymes are extremely versatile catalysts.
4) Enzymes are subject to cellular control. For example, genetic control can
influence the rate of synthesis and final cellular concentration of an enzyme.
Using gene manipulation techniques, it is possible to produce microbial mutants
that are capable of producing large amounts of an enzyme, resulting in high
product formation from readily available substrate. Furthermore, the presence of
6
a certain substrate may induce the conversion of an enzyme from an inactive to
active form (Atkinson and Mavituna, 1991).
Another distinguishing characteristic of enzymes is their frequent need for
cofactors. A cofactor is a nonprotein compound which combines with an other-
wise inactive protein to give a catalytically active complex. The simplest
cofactors are metal ions like Ca2+, Zn2+, Co2+, etc (Bailey, 1986).
2.1.2 Nomenclature and Classification
Individual enzymes selectively catalyze specific reactions. Because of the
high degree of specificity, a system has been established by the Commission on
Enzymes of the International Union of Biochemistry. In this system, as given in
Table 2.1 enzymes are divided into six major classes.
Each of the major classes is further divided into numerical subclasses and
sub-subclasses according to the individual reactions involved (Atkinson and
Mavituna, 1991). Each enzyme has a classification number proposed by the
Enzyme Commission (EC numbers). These classification numbers, prefixed by
EC, which are now widely in use, contain four elements separated by points, with
the following meaning: (i) the first number shows to which of the six main
divisions (classes) the enzyme belongs, (ii) the second figure indicates the
subclass, (iii) the third figure gives the sub-subclass, (iv) the fourth figure is the
serial number of the enzyme in its sub-subclass. For example, the EC number of
β-lactamase is EC 3.5.2.6, which catalyzes the hydrolysis of C-N bond in β-
lactam ring.
2.1.3 Enzyme Activity
The qualitative description of the chemical reactions they catalyze forms
the basis for their classification, while their catalytic activity is quantitatively
expressed in terms of units of activity. The quantitative activity of enzymes give
indication of how much enzyme should be used to achieve a required effect
(product yield) and forms the basis for comparison of several similar enzyme
products (Godfrey and West, 1996). However, a comparison of the activity of
different enzyme preparations is only possible if the assay procedure is
performed exactly in the same way (Faber, 2000). The Commission on Enzymes
7
suggested that a standard unit definition of enzyme activity should be as (Çelik,
2003):
One unit (U) of any enzyme is defined as that amount which will
catalyze the transformation of one micromole of substrate per minute
under defined conditions.
Table 2.1 International classification of enzymes.
No Class Type of reaction catalyzed
1 Oxidoreductases Transfer of electrons
2 Transferases Group-transfer reactions
3 Hydrolases Transfer of functional groups to water
4 Lyases Addition of groups to double bonds or the reverse
5 Isomerases Transfer of groups within molecules to yield
isomeric forms
6 Ligases Formation of C-C, C-S, C-O, and C-N bonds by
condensation reactions coupled to ATP cleavage
2.2 Beta-Lactamases
Bacteria have developed several strategies for escaping the activity of
lethal compounds: enzymatic destruction, decrease of the target sensitivity,
modification of the diffusion barrier(s) and active efflux systems. They utilise
them all to fight beta-lactams but the most common of these resistance
mechanisms is the synthesis of beta-lactamases, enzymes which are usually
secreted into the outer medium by Gram-positive species and into the periplasm
by their Gram-negative counterparts (Matagne et al., 1998). They catalyze the
hydrolysis of β-lactam ring in β-lactam antibiotics, i.e. penicillins and
cephalosporins (Figure 2.1). The products of this hydrolysis reaction are
antibiotically inactive biomolecules.
The synthesis of β-lactamases is observed in a wide range of bacteria in
varying amounts. It has also been found in blue-green algae (Kushner and
8
Breuil, 1977) and yeast (Mehta and Nash, 1978). The presence of this enzyme in
non-bacterial systems suggests that it may have a more widespread role (Çelik,
2003).
Beta-lactamases consist of a single polypeptide chain with the complete
absence of cysteine residue. Specifically β-lactamase from Bacillus licheniformis
consists of 265 amino acids (Çelik, 2003).
In most cases the reported molecular weight for β-lactamases from gram-
positive bacteria is within the range of 28000 – 30000 Da. With benzylpenicillin
as the substrate, typical pH-activity and temperature-activity curves obtained
with β-lactamases from gram-positive bacteria shows maxima in the range of pH
6.0-7.0 and 30°-40°C respectively. The enzyme from Bacillus species are
reasonably stable between pH 3.0-10.0 and are quite thermostable (Çelik,
2003).
Figure 2.1 Hydrolysis of penicillins and cephalosporins by β-lactamase.
R CO NC
C N
C
CH
CS CH3
CH3
O COO-
H
H H
+ H2O C
C N
C
CH
CS CH3
CH3
COOOH
HNR CO
H H
O H
Penicillin Penicilloic acid
R CO N
O
H
H HC
C N
C
CC
CH2
S
CH2R
2
COO-
+ H2O C
C N
C
CC
CH2
S
CH2R
2
COO-OH
HH
HNR CO
OH
Cephalosporin Cephalosporoic acid
β-lactamase
β-lactamase
9
Beta-lactamases are manufactured for the specific assay of penicillins,
destruction of residual penicillins/ cephalosporins in body fluids and culture
media, sterility tests of penicillins, treatment of penicillin sensitivity reactions
and for drug design (White and White, 1997).
2.3 Bioprocess Parameters in Enzyme Production
Any operation involving the transformation of some raw material (biological
or non-biological) into some product by means of microorganisms, animal or
plant cell cultures, or by materials (e.g. enzymes, organelles) derived from
them, may be termed as a “bioprocess” (Moses and Cape, 1991).
In aerobic bioprocesses, there are some important factors that must be
taken into account in order to have high product yield. These are:
1. Microorganism
2. Medium design
3. Bioreactor operation parameters
i. Oxygen transfer rate
* Air inlet rate (Q0/ V)
* Agitation rate (N)
ii. pH and temperature.
2.3.1 Microorganism
In bioprocesses selecting the proper microorganism is very important in
order to obtain the desired product. In choosing the production strain several
aspects have to be considered. Ideally the enzyme is secreted from the cell. This
makes the recovery and purification process much simpler compared to
production of intracellular enzymes, which must be purified from thousands of
different cell proteins and other components. Secondly, the production host
should have a GRAS-status, which means that it is Generally Regarded As Safe.
Thirdly, the organism should be able to produce high amount of the desired
enzyme in a reasonable time frame (Leisola et al., 2001). Traditionally,
identification of the most suitable enzyme source involves screening a wide
range of candidate microorganisms. After screening, most of the industrially
used microorganisms have been genetically modified to overproduce the desired
activity and not to produce undesired side activities.
10
Beta-lactamases are produced by most, if not all, bacterial species, blue
green algae and yeasts. Among many species, Bacillus strains, which fulfill all
the above criteria, are attractive as microbioreactors under well-designed
bioreactor operation conditions due to their secretion ability of large amounts of
enzyme into the bioreactor medium (Çalık et al., 2003b), and this makes the
genus Bacillus more favorable than the others for β-lactamase production.
In the literature concerning β-lactamase production, Sargent et al. (1968)
and Çelik and Çalık (2004) used B. licheniformis; Bernstein et al. (1967),
Kuennen et al. (1980) and Wase and Patel (1987) used B. cereus; whereas,
Hemila et al. (1992), and Sargantanis and Karim (1996, 1998) used B.subtilis.
2.3.1.1 The Genus Bacillus
The rod-shaped bacteria that aerobically form refractile endospores are
assigned to the genus Bacillus. The endospores of the bacilli are resistant to
heat, drying, disinfectants and other destructive agents, and thus may remain
viable for centuries.
The genus Bacillus encompasses a great diversity of strains. Some species
are strictly aerobic, others are facultatively aerobic. Although the majority are
mesophobic, there are also psycrophilic and thermophilic species. Some are
acidophiles while others are alkalophiles. Specifically, B.licheniformis produces
oval endospores that do not swell the mother cell. It is gram positive, is motile
by peritrichous flagella, and produces acids from a range of sugars. It is listed by
the American Food and Drug Administration (FDA) as a GRAS organism.
B.licheniformis is a facultative anaerobe, having pH and temperature tolerance in
the range of 5.0-7.5 and 15°C-50°C respectively. (Priest, 1993; and Laskin and
Lechevalier, 1973).
2.3.1.2 Major Metabolic Pathways and Regulations
A living cell is a complex chemical reactor in which more than 1000
independent enzyme-catalyzed reactions occur. The metabolic reactions tend to
be organized into sequences called metabolic pathways, and that there is some
connection between the pathways by virtue of circular, closed pathways feeding
back on themselves and because of pathway branches which connect one
reaction sequence with another. In this sequence of steps (the pathway), a
11
precursors is converted into a product through series of metabolic intermediates
(metabolites) (Bailey and Ollis 1986). Catabolism is the degradative phase of
metabolism, in which organic nutrient molecules (carbohydrates, fats, and
proteins) are converted into smaller, simpler end products (e.g., lactic acid CO2,
NH3). Catabolic pathways release free energy some of which is converted in the
formation of ATP and reduced electron carriers (NADH and NADPH). In
anabolism, also called biosynthesis, small, simple precursors are built up into
larger and more complex molecules, including lipids, polysaccharides, proteins,
and nucleic acids. Anabolic reactions require the input of energy, generally in the
forms of the free energy of hydrolysis of ATP and the reducing power of NADH
and NADPH (Lehninger, Nelson and Cox, 1993).
Glycolysis and tricarboxylic acid are two central catabolic pathways by
which cells obtain energy from various fuels. Furthermore, the synthesis of
carbohydrates, proteins, lipids and nucleotides are the major anabolic pathways
taking place in the microorganism.
In cell metabolism, groups of enzymes work together in sequential
pathways to carry out a given metabolic process, such as the multi-reaction
synthesis of an amino acid from simpler precursors in a bacterial cell. In such
enzyme systems, the reaction product of the first enzyme becomes the substrate
of the next and so on. In each enzyme system, there is at least one enzyme that
sets the rate of the overall sequence because it catalyzes the slowest or rate-
limiting reaction. These regulatory enzymes exhibit increased or decreased
catalytic activity in response to certain signals. By the action of such regulatory
enzymes, the rate of each metabolic sequence is constantly adjusted to meet
changes in the cell’s demands for energy and for biomolecules required in cell
growth and repair. In most multi-enzyme systems the first enzyme of the
sequence is a regulatory enzyme. The activity of regulatory enzymes is
modulated through various types of signal molecules, which are generally small
metabolites or cofactors. There are two major classes of regulatory enzymes in
metabolic pathways. Allosteric enzymes function through reversible, non
covalent binding of a regulatory metabolite called a modulator. The modulators
for allosteric enzymes may be either inhibitory or stimulatory. An activator is
often the substrate itself, and regulatory enzymes for which substrate and
modulator are identical are called homotropic. When the modulator is a molecule
other than the substrate the enzyme is heterotropic. Allosteric enzymes are
12
significantly different from those of simple non-regulatory enzymes. Some of the
differences are structural. In addition to active or catalytic sites, allosteric
enzymes generally have one or more regulatory or allosteric sites for its
substrate, the allosteric site is specific for its modulator (Lehninger, Nelson and
Cox, 1993).
The second class includes enzymes regulated by reversible covalent
modification. Modifying groups include phosphate, adenosine monophosphate,
adenosine diphosphate ribose, and methyl groups. These are generally
covalently linked to and removed from the regulatory enzyme by separate
enzymes (Lehninger, Nelson and Cox, 1993).
In some multi-enzyme systems the regulatory enzyme is specifically
inhibited by the end product of the pathway, whenever the end product
increases in excess of the cell’s needs. When the regulatory enzyme reaction is
slowed, all subsequent enzymes operate at reduced rates because their
substrates are depleted by mass action. The rate of production of the pathway’s
end product is thereby brought into balance with the cell’s needs. This type of
regulation is called feedback inhibition (Lehninger, Nelson and Cox, 1993).
a) Glycolysis Pathway
In glycolysis a molecule of glucose is degraded in a series of enzyme-
catalyzed reactions to yield two molecules of pyruvate. The breakdown of six-
carbon glucose into two molecules of the three-carbon pyruvate occurs in ten
steps, the first five of which constitute the preparatory phase. In these reactions
glucose is first phosphorylated at the hydroxyl group on C-6. The glucose-6-
phosphate (G6P) thus formed is converted to fructose-6-phosphate (F6P), which
is again phosphorylated, this time at C-1, to yield fructose-1,6-bisphosphate. For
both phosphorylations, ATP is the phosphate donor. Fructose-1,6-bisphosphate is
next split to yield two three-carbon molecules, dihydroxyacetone phosphate and
glyceraldehyde-3-phosphate. The dihydroxyacetone phosphate is isomerized to a
second molecule of glyceraldehyde-3-phosphate; this ends the first phase of
glycolysis. The energy gain comes in the payoff phase of glycolysis. Each
molecule of glyceraldehyde-3-phosphate is oxidized and phosphorylated by
inorganic phosphate to form 1,3-bisphosphoglycerate. Energy is released as two
molecules of 1,3-bisphosphoglycerate are converted into two molecules of
pyruvate (Lehninger, Nelson and Cox, 1993).
13
The flux of glucose through the glycolytic pathway is regulated to achieve
constant ATP levels as well as adequate supplies of glycolytic intermediates that
serve biosynthetic roles. The required adjustment in the rate of glycolysis is
achieved by the regulation of three enzymes: Hexokinase, phosphofructokinase-
1 and pyruvate kinase. Hexokinase which catalyze the conversion of glucose to
G6P is one of the regulatory enzyme in glycolytic pathway, whenever the
concentration of G6P in the cell rises above its normal level, hexokinase is
temporarily and reversible inhibited, bringing the rate of G6P formation balance
with the rate of its utilization and reestablishing the steady-state (Lehninger,
Nelson and Cox, 1993).
The irreversible reaction of F6P to fructose-1,6-bisphosphate catalyzes by
phosphofructokinase-1 (PFK-1) which has several regulatory sites where
allosteric activators or inhibitors bind. ATP is not only a substrate for PFK-1 but
also the end product of the glycolytic pathway. When high ATP levels signal that
the cell is producing ATP faster than it is consuming it, ATP inhibits PFK-1 by
binding to an allosteric site and lowering the affinity of the enzyme for its
substrate fructose-6-phosphate. ADP and AMP, which rise in concentration when
the consumption of ATP outpaces its production, act allosterically to relieve this
inhibition by ATP. These effects combine to produce higher enzyme activity when
F6P, ADP, or AMP builds up, and lower activity when ATP accumulates. Citrate, a
key intermediate in the aerobic oxidation of pyruvate, also serves as an allosteric
regulator of PFK-1; high citrate concentration increases the inhibitory effect of
ATP, further reducing the flow of glucose through glycolysis (Lehninger, Nelson
and Cox, 1993).
The reaction of phosphoenolpyruvate to pyruvate catalyzes by pyruvate
kinase. High concentrations of ATP inhibit pyruvate kinase allosterically, by
decreasing the affinity of the enzyme for its substrate phosphoenolpyruvate
(PEP). Pyruvate kinase is also inhibited by acetyl-CoA and by long-chain fatty
acids. Thus whenever the cell has a high concentration of ATP, or whenever
ample fuels are already available for energy-yielding respiration, glycolysis is
inhibited by the slowed action of pyruvate kinase (Lehninger, Nelson and Cox,
1993).
14
b) Tricarboxylic Acid Cycle
In aerobic organisms, glucose and other sugars, fatty acids, and most of
the amino acids are ultimately oxidized to CO2 and H2O via the tricarboxylic acid
cycle (citric acid cycle). Before they can enter the cycle, the carbon skeletons of
sugars and fatty acids must be degraded to the acetyl group of acetyl-CoA, the
form in which the citric acid cycle accepts most of its fuel input.
To begin a turn of the cycle, acetyl-CoA donates its acetyl group to the
four-carbon compound oxaloacetate to form the six-carbon citrate. Citrate is
then transformed into isocitrate, also six-carbon molecule, which is
dehydrogenated with loss of CO2 to yield the five-carbon compound α-
ketoglutarate. The latter undergoes loss of CO2 and ultimately yields the four-
carbon compound succinate and a second molecule of CO2. Succinate is then
enzymatically converted in three steps into the four-carbon oxaloacetate, with
which the cycle began; thus, oxaloacetate is ready to react with another
molecule of acetyl-CoA to start a second turn. In each turn of the cycle, one
acetyl group enters as acetyl-CoA and two molecules of CO2 leave. Four of the
eight steps in this process are oxidations, in which the energy of oxidation is
conserved, with high efficiency, in the formation of reduced cofactors (NADH and
FADH2) (Lehninger, Nelson and Cox, 1993).
The flow of carbon atoms from pyruvate into and through the citric acid
cycle is under tight regulation at two levels: the conversion of pyruvate into
acetyl-CoA, the starting material for the cycle, and the entry of acetyl-CoA into
the cycle. The cycle is also regulated at the isocitrate dehydrogenase and α-
ketoglutarate dehydrogenase reactions (Lehninger, Nelson and Cox, 1993).
The combined dehydrogenation and de-carboxylation of pyruvate to acetyl-
CoA catalyzes by pyruvate dehydrogenase complex contains three different
enzymes which are pyruvate dehydrogenase (E1), dihydrolipoyl transacetylase
(E2) and dihydrolipoyl dehydrogenase (E3) as well as five different coenzymes or
prosthetic groups- thiamine pyrophosphate (TPP), flavin adenine dinucleotide
(FAD), coenzyme A (CoA), nicotinamide adenine dinucleotide (NAD), and lipoate.
Furthermore, thiamin (in TPP), riboflavin (in FAD), niacin (in NAD), and
pantothenate (in coenzyme A) are vital vitamins of this system. The complex is
strongly inhibited by ATP, as well as by acetyl-CoA and NADH, the products of
15
the reaction. The allosteric inhibition of pyruvate oxidation is greatly enhanced
when long-chain fatty acids are available. AMP, CoA, and NAD+, all of which
accumulate when too little acetate flows into the citric acid cycle, allosterically
activate the pyruvate dehydrogenase complex. Thus this enzyme activity is
turned off when sufficient fuel is available in the form of fatty acids and acetyl-
CoA and when the cell’s ATP concentration and [NADH]/[NAD+] ratio are high,
and turned on when energy demands are high and greater flux of acetyl-CoA
into the citric acid cycle is required (Lehninger, Nelson and Cox, 1993).
There are three strongly exergonic steps in the cycle, those catalyzed by
citrate synthase, isocitrate dehydrogenase, and α-ketoglutarate dehydrogenase.
Each can become the rate-limiting step under some circumstances. The
availability of the substrates for citrate synthase (acetyl-CoA and oxaloacetate)
varies with the metabolic circumstances and sometimes limits the rate of citrate
formation. NADH, a product of the oxidation of isocitrate and α-ketoglutarate,
accumulates under some conditions, and when the [NADH]/[NAD+] ratio
becomes large, both dehydrogenase reactions are severely inhibited by mass
action. Similarly, the malate dehydrogenase reaction is essentially at equilibrium
in the cell, and when [NADH]/[NAD+] ratio is large, the concentration of
oxaloacetate is low, slowing the first step in the cycle. Product accumulation
inhibits all three of the limiting steps of the cycle. The inhibition of citrate
synthase by ATP is relieved by ADP, an allosteric activator of this enzyme. In
short, the concentrations of substrates and intermediates of the citric acid cycle
set the flux through this pathway at a rate that provides optimal concentrations
of ATP and NADH (Lehninger, Nelson and Cox, 1993).
In some organisms acetate can serve both as an energy-rich fuel and as a
source of phosphoenolpyruvate for carbohydrate synthesis. These organisms
have a pathway, the glyoxylate cycle, that allows the net conversion of acetate
to oxaloacetate. In the glyoxylate cycle, acetyl-CoA condenses with oxaloacetate
to form citrate exactly as in the citric acid cycle. The breakdown of isocitrate
does not occur via the isocitrate dehydrogenase reaction, however, but through
a cleavage catalyzed by the enzyme isocitrate lyase, to form isocitrate and
glyoxylate. The glyoxylate then condenses with acetyl-CoA to yield malate in a
reaction catalyzed by malate synthase. The malate subsequently oxidized to
oxaloacetate, which can condense with another molecule of acetyl-CoA to start
another turn of the cycle. The accumulation of intermediates of the central
16
energy-yielding pathways, or energy depletion, results in the activation of
isocitrate dehydrogenase. When the concentration of these regulators falls,
signaling enough flux through the energy yielding citric acid cycle, isocitrate
dehydrogenase is inactivated.
The tricarboxylic cycle and glycolysis are critical catabolic pathways and
also provide important precursors for the biosynthesis of amino acids, nucleic
acids, lipids and polysaccharides. There are, however, other catabolic pathways
taken by glucose that lead to specialized products needed by the cell, and these
pathways constitute part of the secondary metabolism of glucose. One such
pathway is pentose-phosphate pathway which produces NADPH and ribose-5-
phosphate. NADPH is a carrier of chemical energy in the form of reducing power.
The biosynthesis of fatty acids requires reducing power in the form of NADPH to
reduce the double bounds and carbonyl groups of intermediates in this process.
A second function of the pentose phosphate pathway is to generate essential
pentoses, particularly ribose, used in the biosynthesis of nucleic acids
(Lehninger, Nelson and Cox, 1993).
In cells that require primarily NADPH rather than ribose-5-phosphate,
pentose phosphates are recycled into glucose-6-phosphate in a series of
reactions. First, ribulose-5-phosphate (R5P) is epimerized to xylulose-5-
phosphate. Then, in series of rearrangements of the carbon skeletons of sugar
phosphate intermediates, six five-carbon sugar phosphates are converted into
five six-carbon sugar phosphates, completing the cycle and allowing continued
oxidation of glucose-6-phosphate with the production of NADPH. In non-
oxidative reactions of the pentose phosphate pathway convert pentose
phosphates back into hexose phosphates, allowing the oxidative reactions to
continue (Lehninger, Nelson and Cox, 1993).
2.3.1.3 Cell Growth, Kinetics and Yield Factors
Cellular growth is the result of a very large number of chemical reactions
that occur inside individual cells. These reactions include formation of Gibbs free
energy, which is used to fuel all the other reactions, biosynthesis of building
blocks from substrates, polymerization of the building blocks into
macromolecules, and assembly of macromolecules into organelles. In order to
ensure orderly and energy-efficient growth, most of these reactions have to be
17
tightly coupled, and the flux through the various pathways inside the cell is
therefore carefully controlled (Nielsen and Villadsen, 1994).
The rates of formation of biomass and metabolic products can be
determined from measurements of the corresponding concentrations. It is
therefore possible to determine what flows into the total pool of cells and what
flows out of this pool. Volumetric rates can be obtained from the direct
measurements of the concentrations. Often it is convenient to normalize the
rates with respect to the amount of biomass present, since the rates hereby
easily can be compared between fermentation experiments, even when the
amount of biomass changes. Such normalized rates are referred to as specific
rates. The specific growth rate of the total biomass, µ, is also a very important
variable, which is defined as:
dtdC
Cx
x
1=µ (2.1)
where CX is the cell mass concentration (kg m-3), and t is time (h). The
specific growth rate, µ has the units h-1 (Ratledge and Kristiansen, 2001).
Several phases of cell growth are observed in batch culture. Table 2.2
provides a summary of batch cell growth and metabolic activity during the
phases of batch culture.
Table 2.2 Summary of batch cell growth.
Phase Description Specific growth rate
Lag Cells adapt to the new environment µ ≈ 0
Acceleration Growth starts µ < µmax
Growth Growth achieves its maximum rate µ ≈ µmax
Decline Growth slows due to nutrient exhaustion
or build-up of inhibitory products
µ < µmax
Stationary Growth ceases µ = 0
Death Cells lose viability and lyse µ < 0
18
During the exponential growth period –including lag, acceleration, and
growth phases in batch growth, rate of cell growth, rX, is described by the
following equation:
XX
X Cdt
dCr µ== (2.2)
Similarly, substrate consumption rate, -rS and product formation rate, rP, is
described by the following equations respectively:
dtdC
r SS =− (2.3)
dtdCr P
P = (2.4)
Specific substrate consumption and product formation rates are described
as follows:
X
SS C
rq
−= (2.5)
X
PP C
rq = (2.6)
Another class of very important design parameters is the yield coefficients,
which quantify the amount of substrate recovered in biomass and metabolic
products. A list of frequently used yield coefficients is given in Table 2.3.
Yield coefficients are defined based on the amount of consumption of
another material. For example, the yield coefficient of a metabolic product on a
substrate is:
SPY SP ∆
∆−=/ (2.7)
19
where, YP/S is the yield coefficient, P and S are product and substrate,
respectively, involved in metabolism. ∆P is the mass or moles of P produced,
and ∆S is the mass or moles of S consumed. This definition gives an overall yield
representing some sort of average value for the entire culture period. However,
in batch processes, the yield coefficients may show variations throughout the
process for a given microorganism in a given medium, due to the growth rate
and metabolic functions of the microorganism. Therefore, it is sometimes
necessary to evaluate the instantaneous yield at a particular point in time.
Instantaneous yield can be calculated as follows:
S
PSP r
rdtdSdtdP
dSdPY =−=−=
//
/ (2.8)
When yields for fermentation are reported, the time or time period to which
they refer should be stated (Doran, 1995).
Table 2.3 Definition of yield coefficients.
Symbol Definition Unit
YX/S Mass of cells produced per unit mass of
substrate consumed
kg cell kg-1 substrate
YX/O Mass of cells produced per unit mass of
oxygen consumed
kg cell kg-1 oxygen
YS/O Mass of substrate consumed per unit
mass of oxygen consumed
kg substrate kg-1 oxygen
YP/X Mass of product formed per unit mass
of cells produced
kg product kg-1 cell
YP/S Mass of product formed per unit mass
of substrate consumed
kg product kg-1 substrate
YP/O Mass of product formed per unit mass
of oxygen consumed
kg product kg-1 oxygen
20
2.3.2 Medium Design
The general goal in making a medium is to support good growth and/or
high rates of product synthesis. Contrary to intuitive expectation, this does not
necessarily mean that all nutrients should be supplied in great excess.
Most of the products formed by organisms are produced as a result of their
response to environmental conditions, such as nutrients, growth hormones, and
ions. The qualitative and quantitative nutritional requirements of cells need to be
determined to optimize growth and product formation (Shuler and Kargi, 1992).
Nutrients required by cells can be classified in two categories:
1. Macronutrients are needed in concentrations larger than 10-4M. Carbon,
nitrogen, oxygen, hydrogen, sulfur, phosphorus, Mg2+, and K+ are major
macronutrients.
2. Micronutrients are needed in concentrations of less than 10-4M. Trace
elements such as Mo2+, Zn2+, Cu2+, Mn2+, Fe2+, Ca2+, Na2+, vitamins,
growth hormones, and metabolic precursors are micronutrients.
Table 2.4 lists the eight major macronutrients, their physiological functions,
typical amount required in fermentation broth, and common sources.
For any bacterium to be propagated for any purpose it is necessary to
provide the appropriate biochemical and biophysical environment. The
biochemical (nutritional) environment is made available as a culture medium,
and depending upon the special needs of particular bacteria a large variety and
types of culture media have been developed with different purposes and uses
(Todar, 2000). There are two major types of growth media, defined and
complex, depending on their composition. A chemically defined (synthetic)
medium is one in which chemical composition is well known. Such media can be
constructed by supplementing a mineral base with the necessary carbon,
nitrogen, and energy sources as well as any necessary vitamins. The primary
advantage of defined media is that the results are more reproducible and the
operator has better control of the fermentation. Complex media contain natural
compounds whose chemical composition is not exactly known. A complex
medium usually can provide the necessary growth factors, vitamins, hormones,
and trace elements.
21
Com
mon S
ourc
e
Glu
cose
, su
crose
fru
ctose
(f
or
def
ined
med
ium
)
Am
monia
, am
monia
sal
ts,
pro
tein
s, a
min
o a
cids
Car
bon
com
pou
nds
such
as
carb
ohyd
rate
s
Spar
gin
g a
ir o
r su
rfac
e ae
ration
Sulp
hat
e sa
lts
Inorg
anic
phosp
hat
e sa
lts
(KH
2PO
4,
K2H
PO4)
Inorg
anic
pota
ssiu
m s
alts
(K
H2PO
4,
K2H
PO4,
K3PO
4)
MgSO
47H
2O
, M
gCl 2
Req
uired
Conce
ntr
atio
n
(mol l-1
)
> 1
0-2
10
-3
10
-4
10
-4 t
o 1
0-3
10
-4 t
o 1
0-3
10
-4 t
o 1
0-3
Phys
iolo
gic
al Fu
nct
ion
Const
ituen
t of
org
anic
cel
lula
r m
ater
ial. O
ften
the
ener
gy
sourc
e.
Const
ituen
t of
pro
tein
s, n
ucl
eic
acid
s, a
nd c
oen
zym
es.
Const
ituen
t of
org
anic
cel
lula
r m
ater
ial an
d w
ater
.
Const
ituen
t of
org
anic
cel
lula
r m
ater
ial an
d w
ater
. Req
uired
for
aero
bic
res
pirat
ion.
Const
ituen
t of
pro
tein
s an
d c
erta
in c
oen
zym
es.
Const
ituen
t of
nucl
eic
acid
s, p
hosp
holip
ids,
nucl
eotides
and
cert
ain c
oen
zym
es.
Princi
pal
inorg
anic
cat
ion in t
he
cell
and c
ofa
ctor
for
som
e en
zym
es.
Cofa
ctor
for
man
y en
zym
es a
nd c
hlo
rophyl
ls a
nd p
rese
nt
in t
he
cell
wal
ls a
nd m
embra
nes
.
Tab
le 2
.4 T
he
maj
or
mac
ronutr
ient
elem
ents
, th
eir
phys
iolo
gic
al f
unct
ions,
gro
wth
req
uirem
ents
and c
omm
on s
ourc
es.
Ele
men
t
Car
bon
Nitro
gen
Hyd
rogen
Oxy
gen
Sulfur
Phosp
horu
s
Pota
ssiu
m
Mag
nes
ium
22
In the study of Çelik and Çalık (2004), the effects of medium components
for β-lactamase production by Bacillus species were investigated and medium
containing 1.2 kg m-3 (NH4)2HPO4, 8.0 kg m-3 yeast extract, 10 kg m-3 glucose
and salt solution gave maximum β-lactamase production. In the study of Hemila
et al. (1992), the effect of glucose was investigated for improving β-lactamase
production in a strain of B.subtilis, and the addition of 60 kg m-3 glucose and 100
mM potassium phosphate was defined as the favorable condition for higher
yields and stability, but with the disadvantage of retardation of growth in the
exponential phase.
2.3.3 Bioreactor Operation Parameters
Bioreactor operation parameters i.e., oxygen transfer rate, pH, and
temperature influences the patterns of microbial growth and product formation.
2.3.3.1 Temperature
Temperature is an important factor affecting the performance of cells. As
the temperature is increased toward optimal growth temperature, the growth
rate approximately doubles for every 10°C increase in the temperature. Above
the optimal temperature range, the growth rate decreases and thermal death
may occur. Temperature also affects product formation. However, the
temperature optimum for growth and product formation may be different. When
temperature is increased above the optimum value, the maintenance
requirements of cells increase. The yield coefficient is also affected by
temperature (Shuler and Kargi, 1992).
In the literature concerning β-lactamase production, Wase and Patel (1987)
and Sargent et al. (1968) conducted β-lactamase production at T=30°C and
Sargantanis and Karim (1996, 1998) at T=37°C, without investigating the effect
of temperature. Bernstein et al. (1967) investigated the effect of temperature on
β-lactamase production in the range T=18°C-46°C, and reported that the basal
level of β-lactamase production in an inducible strain of B. cereus reaches a
maximum at T=42°C. They have also proposed that culturing at 42°C and
lowering the temperature to 37°C leads to an increase in β-lactamase production.
Kuennen et al. (1980) also investigated the effect of temperature, and reported
that β-lactamase activity was relatively constant when a constitutive strain of B.
23
cereus was grown at a temperature range of 33°C to 42°C, above which a rapid
decrease in activity was observed. In the study with B.subtilis β-lactamase by
Hemila et al. (1992), it was concluded that in the range 27°C to 40°C, 30°C was
the optimum cultivation temperature for β-lactamase production. In a more
recent study, Çelik and Çalık (2004) investigated the effects of temperature in
the range T=29°C-37°C, and T=32°C was found to be the most favorable
condition for β-lactamase production by B.licheniformis.
2.3.3.2 pH
Microbial cells have a remarkable ability to maintain the intracellular pH at
a constant level even with large variations in the pH of the extracellular medium,
but only at the expense of a significant increase in the maintenance demands,
since Gibbs free energy has to be used for maintaining the proton gradient
across the cell membrane (Nielsen and Villadsen, 1994).
In most fermentation processes, pH can vary substantially. Often the
nature of the nitrogen source can be important. Also, pH can change due to the
production of organic acids, utilization of acids (particularly amino acids). Thus,
pH control by means of a buffer or an active pH control system can be
important depending on the nature of the bioprocess, since , some bioprocesses
require controlled pH conditions, while others might require uncontrolled pH
operations, in order to increase the product yield and selectivity (Çalık et
al.,2002).
In the study by Sargent et al. (1968), specific β-lactamase activity of cells
was shown to be constant irrespective of pH over the range of pH 5.5 to 7.5.
However, the fraction of the total enzyme secreted into the extracellular medium
was favorable around pH 7.5. In the study with B.subtilis β-lactamase by Hemila
et al. (1992), it was concluded that in the pH range 5.8 to 7.4, pH 6.0 was the
optimum cultivation pH for β-lactamase production. Sargantanis and Karim
(1996) stated that pH control was not beneficial for β-lactamase productivity,
and conducted their experiments at an initial pH of 7.0, without investigating its
effect (Çelik, 2003). In a more recent study, Çelik and Çalık (2004) investigated
the effects of pH in the range of 5.8 - 7.2 in media with NaH2PO4 - Na2HPO4
buffer having a buffering capacity of 0.02 M, and in media without buffer, where
the initial pH was set by the addition of either NaH2PO4 or Na2HPO4. The
24
uncontrolled pH operation with an initial pH of 6.25 was found to be the most
favorable condition for β-lactamase production by B.licheniformis.
2.3.3.3 Oxygen Transfer Rate
Oxygen is an essential element for aerobic growth and product formation.
The transfer of oxygen into the microbial cell in aerobic fermentation processes
affects product formation by influencing metabolic pathways and changing
metabolic fluxes (Çalık et al., 1999). In general, according to cell growth
conditions and metabolic pathway analysis, some bioprocesses require high
oxygen transfer rate conditions while others require controlled oxygen transfer
rates in order to regulate oxygen uptake rates (Çalık et al., 1998). Oxygen
transfer rate can be adjusted by either changing the air inlet rate or agitation
rate.
In aerobic processes, oxygen is a key substrate and because of its low
solubility in aqueous solutions a continuous transfer of oxygen from the gas
phase to the liquid phase is decisive for maintaining the oxidative metabolism of
the cells. An overview of mass transfer phenomena in a fermentation process is
given in Figure 2.2, which summarizes all the individual steps involved in oxygen
transport from a gas bubble to the reaction site inside the individual cells (Bailey
and Ollis, 1986). The steps are:
1. Diffusion of oxygen from the bulk gas to the gas-liquid interface.
2. Transport across the gas-liquid interface.
3. Diffusion of oxygen through a relatively stagnant liquid region
adjacent to the gas bubble, i.e., from the gas-liquid interface to the
well-mixed bulk liquid.
4. Transport of oxygen through the well-mixed liquid to a relatively
unmixed liquid region surrounding the cells.
5. Diffusion through the stagnant region surrounding the cells
6. Transport from the liquid to the pellet, cell aggregate, etc.
25
7. Diffusive transport of oxygen into the pellet, etc.
8. Transport across the cell envelope
9. Transport from the cell envelope to the intracellular reaction site, e.g.,
the mitochondria.
Figure 2.2 Overview of steps in the overall mass transfer of oxygen from a gas
buble to the reaction site inside the individual cells.
When cells are dispersed in the liquid, and the bulk fermentation broth is
well mixed, the transport through the well-mixed liquid is normally very rapid.
Furthermore steps five, six and seven are relevant only for processes in which
pellets or cell aggregates appear. Transport resistance within the cell is normally
also neglected, because of the small size of most cells (Nielsen and Villadsen
1994). Therefore mass transfer of gas to liquid, normally modeled by the two-
film theory, is of prime importance. An expression for oxygen transfer rate
(OTR) from gas to liquid is given by the following equation:
26
)( *OOL CCaKOTR −= (2.9)
Since solubility of oxygen in aqueous solutions is very low, the liquid phase
mass transfer resistance dominates, and the overall mass transfer coefficient, KL,
is approximately equal to liquid phase mass transfer coefficient, kL.
The rate of oxygen transfer in fermentation broth is influenced by several
physical and chemical factors. These are bubble characteristics, rheological
properties of the medium, air inlet rate, agitation rate, antifoam agents,
temperature and the presence of cells and solutes that change either the value
of KLa, or the oxygen uptake rate of the cell. Therefore, oxygen uptake rate
(OUR) and volumetric mass transfer coefficient (KLa) are known as the oxygen
transfer characteristics.
a) Oxygen Uptake Rate
The rate at which oxygen is consumed by cells in fermenters determines
the rate at which it must be transferred from the gas to liquid. Many factors can
influence the total microbial oxygen demand. The more important of these are
cell species, culture growth phase, carbon nutrients, pH, and the nature of the
desired microbial process, i.e., substrate utilization, biomass production, or
product yield. The carbon nutrient affects oxygen demand in a major way. For
example, glucose is generally metabolized more rapidly than other carbohydrate
substances. The component parts of oxygen utilization by the cell include cell
maintenance, respiratory oxidation for further growth, and oxidation of
substrates into related metabolic end products. In examining metabolic
stoichiometry, oxygen utilization for growth is typically coupled directly to the
amount of carbon-source substrate consumed (Bailey and Ollis 1986). Oxygen
uptake rate (OUR), -r0, per unit volume of broth is given by
XCqr 00 =− (2.10)
where qo is the specific oxygen uptake rate, kg kg-1 DW h-1, Cx is the cell
concentration, kg DW m-3.
27
For the design of aerobic biological reactors correlations of data more or
less approximating the situation of interest are frequently used to establish
whether the slowest process step is the oxygen transfer rate or the rate of
cellular utilization of oxygen (or other limiting substrate). The maximum possible
mass-transfer rate is simply that found by setting C0 = 0 in equation (2.9): all
oxygen entering the bulk solution is assumed to be rapidly consumed. The
maximum possible oxygen utilization rate can be found by the following
equation:
0/maxmax0 / Xx YCr µ=− (2.11)
Evidently, if maximum possible oxygen transfer rate is much larger than
maximum possible oxygen utilization rate, the main resistance to increased
oxygen consumption is microbial metabolism and the reaction appears to be
biochemically limited. Conversely, the reverse inequality apparently leads to C0
near zero, and the reactor seems to be in the mass-transfer-limited mode. The
situation is actually slightly more complicated. In general above some critical
bulk oxygen concentration the cell metabolic machinery is saturated with
oxygen. In this case, sufficient oxygen is available to accept immediately all
electron pairs which pass through the respiratory chain, so that some other
biochemical process within the cell is rate-limiting (Bailey and Ollis 1986).
b) Volumetric Mass Transfer Coefficient
The product of the overall mass transfer coefficient KL and the specific
interfacial area a is called the volumetric mass transfer coefficient KLa. Due to
the difficulties in the determination of KL and a individually, their product is
normally used to specify the gas-liquid mass transfer.
A large number of different empirical correlations for the volumetric mass
transfer coefficient KLa have been presented in the literature. Most of these
correlations can be written in the form:
αβ
sR
GL V
VP
kaK
= (2.12)
28
where the parameters are specific for the considered system, i.e. for the
bioreactor design. Thus for different stirrers and different tank geometry the
parameter values may change significantly, and a certain set of parameters can
be reasonably used only when studying a system which the parameters were
originally derived. Some of the parameter values reported in the literature for
stirred tanks are listed in Table 2.5.
29
Ref
eren
ce
Moo-Y
oung a
nd B
lanch
(1
981)
Linek
et
al.
(1987)
Moo-Y
oung a
nd B
lanch
(1
981)
van’t R
iet
(1979)
Moo-Y
oung a
nd B
lanch
(1
981)
Moo-Y
oung a
nd B
lanch
(1
981)
van’t R
iet
(1979)
Çalık
et
al.
(1998)
Agitat
or
Six
-bla
ded
Rush
ton
turb
ines
Six
-bla
ded
Rush
ton
turb
ines
Var
ious
agitat
ors
Not
spec
ifie
d
Six
-bla
ded
Rush
ton
turb
ines
Var
ious
agitat
ors
Not
spec
ifie
d
Not
spec
ifie
d
β 0.4
0.5
93
0.4
75
0.4
0.7
0.4
75
0.7
0.7
α 0.5
0.4
0.4
0.5
0.3
0.4
0.2
0.2
k 0.0
25
0.0
0495
0.0
1
0.0
26
0.0
018
0.0
2
0.0
02
0.0
0525
Eq #
1
2
3
4
5
6
7
8
Tab
le 2
.5 P
aram
eter
val
ues
for
the
empiric
al c
orr
elat
ion o
f K
La.
Med
ium
Coal
esci
ng
Nonco
ales
cing
30
Although KLa is difficult to predict, it is a measurable parameter. There are
several methods for measuring the volumetric mass transfer coefficient KLa for
oxygen. A few of the best known methods are Sulphite Method, Gas Analysis
Method and Dynamic Method.
Dynamic Method is a widely used simple method that can be applied during
a fermentation process to determine the value of KLa experimentally. The
method is based on an unsteady state mass balance for oxygen given by the
following equation:
XOOLO CqCCaK
dtdC
0* )( −−= (2.13)
As shown in Figure 2.3, at some time t0, the broth is de-oxygenated by
stopping the air flow. During this period, dissolved oxygen concentration, Co0,
drops, and since there is no oxygen transfer, equation (2.13) becomes:
0rdtdCO = (2.14)
Using equation (2.14) in region-II of Figure 2.3, oxygen uptake rate, -r0,
can be determined.
Air inlet is then turned back on, and the increase in CO is monitored as a
function of time. In this period, region-III, equation (2.13) is valid. Combining
equations (2.10) and (2.13) and rearranging,
*0 )(1
OO
LO Cr
dtdC
aKC +−−= (2.15)
From the slope of a plot of CO versus (dCO/dt – r0), KLa can be determined
(Figure 2.4).
31
Figure 2.3 Variation of dissolved oxygen concentration with time in dynamic
measurement of KLa.
Figure 2.4 Evaluating KLa using the Dynamic Method
Co
(dCO/dt-rO)
Slope= -1/KLa
Air off
Air
I II III
Co
Co0
timet0 t1
32
The Dynamic Method can also be applied to conditions under which there is
no reaction, i.e., r0=0 (Nielsen and Villadsen, 1994). In this case, the broth is
de-oxygenated by sparging nitrogen into the vessel. Air inlet is turned back on
and again the increase in Co is monitored as a function of time. Modifying
equation (2.15)
*1O
O
LO C
dtdC
aKC +−= (2.16)
From the slope of a plot of CO versus dCO/dt, the physical mass transfer
coefficient, KLa0, can be determined.
The effect of oxygen transfer conditions on β-lactamase production by
Bacillus species was investigated by Sargantanis and Karim (1996, 1998). They
mainly focused on the performance of dissolved oxygen (DO) control strategy,
and compared β-lactamase activities observed at different dissolved oxygen
levels, which were kept constant during the bioprocess using an adaptive pole
placement control algorithm. They performed the experiments at 3%, 5%, 8%
and 15% constant dissolved oxygen levels and reported the highest productivity
of β-lactamase at the highest DO level (15%), but that the rate of β-lactamase
degradation by proteases was the highest at this level also, without giving the
protease activities. Therefore, they concluded that β-lactamase production was
much higher at low DO levels (3%), although it occurred at a later stage of the
fermentation, and that limited growth conditions favored long-term β-lactamase
production.
In the recent study of Çelik and Çalık (2004), oxygen transfer
characteristics (-r0, KLa) of the bioprocess for β-lactamase production by
B.licheniformis were investigated in a semi-defined medium containing glucose,
(NH4)2HPO4, yeast extract and the salt solution, at pH0 = 6.0, T= 32°C at
Q0/V=0.5 vvm and N=500 min-1 oxygen transfer conditions and found that
throughout the bioprocess, overall oxygen transfer coefficient (KLa) varied
between 0.008-0.016 s-1; oxygen uptake rate varied between 0.001-0.003 mol
m-3 s-1.
Related with the production of other biomolecules using Bacillus
licheniformis, effects of oxygen transfer were investigated in the production of
33
serine alkaline protease by Çalık et al. (1999) at nine different oxygen transfer
conditions by forming a 3x3 matrix using three agitation rates N=150, 500, 750
min-1 and three air inlet rates QO/VR=0.2, 0.5, 1.0 vvm with the initial substrate
concentration CC=9.0 kg m-3 by using a laboratory-scale 3.5 dm3 batch
bioreactor consisted of a system of working volume 2.0 dm3 equipped with two
four-blade Rushton turbines, and dissolved oxygen, temperature, pH, foam, air–
inlet and stirring rate measurements and control. In the bioreactor the oxygen
uptake rate (OUR) values as well as the oxygen transfer rate (OTR) increased
with the increasing oxygen transfer, i.e. QO/VR and N, up to the medium oxygen
transfer condition, QO/VR= 0.5 vvm and N=750 min-1. Nevertheless, at higher
oxygen transfer conditions the cell growth, and consequently the OUR and OTR
decreased. The impact of the further increase in QO/VR and/or N after QO/VR=
0.5 vvm and N=750 min-1 condition increases the shear fields in the bioreactor;
and the exposure of the bacilli to higher shear fields at high oxygen transfer
conditions causes considerable dynamic influences that decrease the OUR as well
as the OTR and consequently perturbs the metabolism of B.licheniformis. With
the carbon source citrate, the consumption rate of the substrate increases with
increasing agitation rate and air inlet rate, and cell concentration was the highest
at low oxygen transfer condition.
2.4 Metabolic Flux Analysis
Metabolic flux analysis (MFA) is based on calculation of intracellular
reaction network rates through various reaction pathways -either theoretical or
by using elaborate experimental data on uptake, excretion, secretion rates,
biosynthetic requirements with metabolic stoichiometry- by solving the mass-
balance-based mathematical model developed for the bioreaction network
components, either at pseudo-steady state or at steady-state. MFA describes the
interactions between the cell and the bioreactor with proper emphasis on the
metabolic state and the metabolic process in order to fine-tune the bioreactor
performance. This analysis can be used to find the critical branch points and
bottlenecks in the overall flux distributions, for modifying the medium
composition, for improving the bioreactor operation conditions, moreover for
calculating the theoretical metabolic capacities of the microorganism, and for
selecting the host microorganism (Çalık et al., 2002).
34
2.4.1 Modelling of Bioreaction Network for Metabolic Flux Analysis
Conceptually, the cell functions as the semibatch micro-bioreactor with
volume V wherein the biochemical reactions take place; and, a small number of
compounds of the intracellular biochemical reaction network (e.g substrates,
oxygen, H+, H2O, CO2, amino acids, organic acids of the glycolysis or
gluconeogenesis pathways and the tricarboxylic acid (TCA) cycle, and
extracellular proteins) is exchanged or transferred with facilitated and active
transport mechanisms between the metabolic system, and the bioreactor
medium which is defined as the environment. Therefore, the reactions that
represent the specific properties of the microorganism used should be studied;
consequently, an idea of the main biochemical processes that occur inside the
organism and an idea about the chemical reactants which are involved are
indeed needed. In order to describe the intracellular metabolic reaction network
in chemical detail by an increased number of reactions, of which the
stoichiometry is precisely known, the biochemical reactions of the biochemical
reaction network need to be determined and studied one-by-one. Consequently,
the biochemical reaction network, including the cell synthesis reaction using the
complete chemical composition data of the cell and the product synthesis
reaction, must be set up. Thus, starting from the site that the substrate(s)
enters into the carbon mechanism, the biochemical reaction network should
consider all the relevant bioreactions of the central carbon metabolism, i.e., the
glycolysis and the gluconeogenesis pathways, the pentose phosphate pathway
(PPP), the TCA cycle including the glyoxylate shunt, and the anaplerotic
reactions. The overall pathway can be simplified based on a comparison of the
extracellular growth compounds and the intracellular chemical compounds by
lumping some reactions into single ones without loosing representation accuracy.
Moreover, some major assumptions can also be incorporated in the model. In
this context in the second step, for the each metabolite of the intracellular
reaction network one equation is obtained which is defined as the algebraic sum
of all the conversions in the defined reactions and transport equals to the
accumulation of the intracellular metabolite in the micro-bioreactor (cell), as
follows (Çalık et al., 2002):
dtCdrr iTiRi /)(=± (2.17)
35
where, rRi is the net-reaction and rTi is the net-transfer rate; and d(Ci)/dt is
the accumulation rate of the intracellular metabolite within cell. In the mass flux
balance-based analysis, equation (2.17) can be written in a vector form as
follows:
)()(* tctrA = (2.18)
where, A is the stochiometric coefficients matrix of the metabolic network, r(t)
is the vector of reaction fluxes and c(t) is the metabolite accumulation vector.
The elements of c(t) are divided into two subvectors.
)()()( 21 tctctc += (2.19)
where c1(t) and c2(t) corresponding to extracellular and intracellular metabolite
accumulation vectors, respectively. Due to the very high turnover of the pools of
most metabolites, the concentrations of the different metabolites pools rapidly
adjusted to new levels, even after large perturbations in the fermentation broth.
Therefore, it is reasonable to use the pseudo-steady state (PSS) approximation
for the intracellular metabolites, c2(t)=0. Thus, equation (2.18) can be written as
(Çalık et al., 2001):
)()(* 1 tctrA = (2.20)
For the corresponding vector equation (2.20), the stoichiometric coefficients
matrix of m x n need to be constructed, where m is the number of the
metabolites in the bioreaction network and n is the number of the reactions.
2.4.2 Solution of the Mathematical Model
The A matrix can be determined on the basis of the biochemistry of the
microorganism. If m > n the solution of the model gives the approximate exact
solution. The solution of equation 2.20 can be determined by a constrained least-
squares approach with the objective of minimising the sum of squares of
residuals from the stoichiometric mass balance. Nevertheless, if m<n, metabolic
flux distributions can be obtained by minimising or maximising the objective
function, whereupon the best metabolic pathway utilisation that would fulfill the
36
stated objective is obtained. If m<n, the mathematical formulation for the
objective function Z is:
ii rZ α∑= (2.21)
where, Z is a linear combination of the fluxes ri , and αi is the coefficient of
the component-i in the stoichiometric equation of the corresponding reaction.
In least-squares method matrix is solved and a unique solution is obtained (Çalık
et al., 2002).
Metabolic flux analysis has been successfully applied to a number of
fermentation processes. In general, the literature reports on the metabolic flux
analysis for four enzymes, serine alkaline protease (SAP) (Çalık et al., 1999,
2001) , neutral protease (Çalık et al., 2001), amylase (Amy) (Çalık et al., 2001;
Nielsen et al., 1999), and glucoamylase (Nielsen et al., 1996).
Related with an enzyme production by Bacillus species, Bacillus
licheniformis (Çalık and Özdamar, 1999; Çalık et al., 1999, 2000, 2001), was the
only microorganism studied for the metabolic flux analysis. Çalık and Özdamar
(1999) investigated the biochemistry of Bacillus licheniformis and developed a
detailed mass flux balance-based stoichiometric model that contains m=105
metabolites and n=148 reaction fluxes to obtain the intracellular metabolic flux
distributions for serine alkaline protease production by using batch experimental
data in which citrate was used as the carbon source. The model was solved by
using simplex optimization algorithm in which the objective function was defined
as the difference between protease synthesis rate and protease secretion rate.
The results indicated that the intracellular amino acid fluxes played an important
role in the serine alkaline protease fermentation process. Çalık et al. (1999)
reported the influence of bioreactor operation conditions, i.e. the effects of
oxygen-transfer rate on the intracellular metabolic flux distributions, in
B.licheniformis under well-defined batch bioreactor conditions to evaluate the
effects on the metabolism of the bacilli in serine alkaline protease fermentation
process. They reported that the flux partitioning in the TCA cycle at α-
ketoglutarate towards glutamate group and at oxaloacetate towards aspartate
group amino acids were dependent mainly on the oxygen transfer rate,
moreover, the flux of the anaplerotic reactions that connects the TCA cycle either
37
from malate or oxaloacetate to the gluconeogenesis pathway via the main
branch point pyruvate was also influenced by the oxygen transfer rate. Further,
with the decrease in the oxygen transfer rate, the intracellular flux values after
glycerate 3-phosphate in the gluconeogenesis pathway and the specific growth
rate decreased and the total ATP generation rate increased with the increase in
oxygen transfer rate. Lastly they mentioned that the pathway towards the
aspartic acid family amino acids which is important for sporulation that precedes
the serine alkaline protease synthesis were all active throughout the bioprocess.
38
CHAPTER 3
MATERIALS AND METHODS
3.1 Chemicals
Benzylpenicillin (penicillin G) was purchased from Sigma Chemical
Company, St. Louis, Missouri, USA. All other chemicals were analytical grade,
and obtained either from Sigma Ltd., Difco Laboratories, or Merck Ltd.
3.2 The Microorganism
Bacillus licheniformis 749/C (ATCC 25972) was used as the microbial
source of β-lactamase (EC 3.5.2.6). The microorganisms, which were freeze
dried when received, were kept at -20ºC, and brought to an active state by
incubating for 30 min, at 30ºC, in a liquid medium, V=0.3ml, that contained (kg
m-3): soytryptone, 5; peptone, 5; MnSO4.2H2O, 0.010. Afterwards, the
microorganisms were inoculated onto a solid medium, and stored at 4ºC.
3.3 The Solid Medium
The microorganisms, stored on agar slants at 4ºC, were inoculated onto
the newly prepared agar slants under sterile conditions, and they were incubated
at 30ºC for 24h. The composition of the solid medium for β-lactamase production
by Bacillus sp. is given in Table3.1 (Çelik, 2003).
Table 3.1 The composition of the solid medium for Bacillus sp.
Compound Concentration, kg m-3
Soytryptone 5.00
Peptone 5.00
MnSO4.2H2O 0.01
Agar 15.00
39
3.4 The Precultivation Medium
Microorganisms grown in the solid medium for 24 h, were inoculated into
precultivation medium, and incubated at 37ºC and N=200 min-1 for 3.5 h.
Microorganism growth was conducted in orbital shakers under agitation and
heating rate control, using air-filtered Erlenmeyer flasks 150 ml in size that had
working volume capacities of 33 ml. The composition of the precultivation
medium for cell growth and β-lactamase production is given in Table 3.2 (Çelik,
2003).
Table 3.2 The composition of the precultivation medium.
Compound Concentration, kg m-3
Soytryptone 15.0
Peptone 5.00
Na2HPO4 0.25
CaCl2 0.10
MnSO4.2H2O 0.01
3.5 The Production Medium
When the microorganism concentration in the precultivation medium
reached to 0.30 kg m-3, the microorganisms were inoculated to the production
medium, contained either in the laboratory scale bioreactor (V=150 ml) or pilot
scale bioreactor (V=3.0 dm3), with an inoculation ratio of 1/10.
Laboratory scale batch fermentations were conducted in agitation and
heating rate controlled orbital shakers at an agitation rate of 200 min-1 and a
cultivation temperature of 37ºC, using air filtered 150 cm3 shake bioreactor that
contained VR = 33 cm3 reference medium whose composition is given in Table
3.3 (Çelik, 2003), unless otherwise stated.
The laboratory scale experiment results enabled the design of the defined
medium for the β-lactamase production in terms of the initial carbon and
nitrogen source concentrations and bioreactor operation conditions. Pilot scale β-
lactamase fermentation were accomplished using this optimized medium in 3.0
40
dm3 batch bioreactor (Braun CT2-2), having a working volume of 0.5-2.0 dm3
and a diameter of 12.1 cm, and consisting of temperature, pH, foam, stirring
rate and dissolved oxygen controls. The bioreactor utilized an external cooler,
steam generator and a jacket around the bioreactor for sterilization and
temperature control. The bioreactor was stirred with two four-blade Rushton
turbines with a diameter of 5.4 cm, and consisted of four baffles and a sparger.
All the medium components except the salt solution were steam sterilized
at 121°C for 20 min, glucose being sterilized separately. The micronutrients all
together, referred to as the salt solution, was filter sterilized with a sterile filter
of 0.2 µm pore size.
Table 3.3 The composition of the reference production medium.
Macronutrients Concentration, kg m-3
Glucose 8.0
(NH4)2HPO4 4.7
Micronutrients
(salt solution) Concentration, kg m-3
MgSO4.7H2O 0.25
FeSO4.7H2O 1.0 x 10-3
ZnSO4.7H2O 1.0 x 10-3
MnSO4.H2O 7.5 x 10-5
CuSO4.5H2O 1.0 x 10-5
3.6 Analysis
Throughout the bioprocess, samples were taken at different cultivation
times. After determining the cell concentration, the medium was centrifuged at
13500 min-1 for 10 min to separate the cells. Supernatant was used for the
determination of β-lactamase activity. In pilot scale experiments, besides β-
lactamase activity, cell, glucose, β-lactamase and SAP concentrations; amino
acid and organic acid concentrations were determined.
41
3.6.1 Cell Concentration
Cell concentrations based on dry weights were measured with a UV-Vis
spectrophotometer (Thermo Spectronic, Heλios α) using a calibration curve
(Appendix A) obtained at 600 nm.
3.6.2 Beta-Lactamase Activity
Beta-lactamase activity was determined by measuring the hydrolysis of
benzylpenicillin. Samples from the culture broth was harvested by centrifugation
(Sigma 1-15) at 13,500 g for 10 min. Fresh substrate solutions were prepared
daily and maintained at 30°C, by dissolving 0.25 kg m-3 benzylpenicillin in 0.1 M
phosphate buffer, pH 7.0. 0.1 cm3 sample of centrifuged culture supernatant,
diluted properly, was added to 3 cm3 of substrate solution and immediately
analyzed, by following the change in absorbance in one minute at 232 nm with a
UV spectrophotometer (Thermo Spectronic, Heλios α) (Wase and Patel, 1987).
One unit of β-lactamase activity was defined as the amount of enzyme that could
hydrolyze 1µmol of benzylpenicillin at 30°C and pH 7.0 in one minute (Çelik,
2003), (Appendix B).
3.6.3 Beta-Lactamase and Serine Alkaline Protease Concentrations
β-lactamase and serine alkaline protease concentrations were determined
with a high performance capillary electrophoresis at 214 nm (Waters HPCE,
Quanta 4000E). The samples were analyzed at 12kV and 15°C with a negative
power supply by hydrostatic pressure injection, using an electrolyte containing
Z1-Methyl (Waters) salt in 100 mM borate buffer (Çalık et al., 1998). The
enzyme concentrations were calculated from the chromatogram, based on the
chromatogram of the standard enzyme solutions. The calibration curves for β-
lactamase and serine alkaline protease concentrations are given in Appendix C
and Appendix D respectively.
3.6.4 Reduced Sugar Concentration
Reduced sugar, glucose, concentration was determined by the DNS
(dinitrosalisylic acid) method (Miller, 1959) at 550 nm with a UV
spectrophotometer. The calibration curve and the preparation method of the
DNS solution are given in Appendix E and F, respectively. The method used in
analysis of samples and preparation of the calibration curve is given below:
42
1. 3 cm3 of DNS solution was added into test tubes containing 1 cm3 of
sample at different glucose concentrations.
2. The test tubes were put into boiling water for 5 min and then into ice
for another 5 min.
3. The sample passing through the same steps but do not contain any
reducing sugar is used as blank and the absorbance values of the
samples were measured by a UV spectrophotometer at 550 nm (Çelik,
2003).
3.6.5 Amino Acid Concentrations
Amino acid concentrations were measured with an amino acid analysis
system (Waters, HPLC), using the Pico Tag method (Cohen, 1983). The method
is based on reversed phase HPLC, using a precolumn derivation technique with a
gradient program developed for amino acids. The amino acid concentrations
were calculated from the chromatogram, based on the chromatogram of the
standard amino acids solution. The analysis was performed under the conditions
specified below:
Column :Amino acid analysis column
(Nova-Pak C18, Millipore)
Column dimensions :3.9 mm x 30 cm
System :Reversed phase chromatography
Mobile phase flow rate :1 ml/min
Column temperature :38 °C
Detector and wavelength :UV/VIS, 254 nm
Injection volume :4 µl
Analysis period :20 min
3.6.6 Organic Acid Concentrations
Organic acid concentrations were determined with a high performance capillary
electrophoresis at 254 nm (Waters HPCE, Quanta 4000E). The samples were
analyzed at 20kV and 15°C with a negative power supply by hydrostatic pressure
43
injection, using an electrolyte containing 5mM potassium hydrogen phtalate and
0.5mM OFM Anion Bt (Waters) as the flow modifier at pH=5.6 (for α-ketoglutaric
acid, acetic acid, malic acid, fumaric acid, succinic acid, lactic acid, oxalacetate
and gluconic acid) and at pH=7.0 (for, pyruvic acid, citric acid, lactic acid,
gluconic acid) ( Çalık et al., 1998).
3.6.7 Liquid Phase Mass Transfer Coefficient and Oxygen Uptake Rate
In order to determine the liquid phase mass transfer coefficient and oxygen
uptake rate in the β-lactamase production process, the Dynamic Method (Rainer
1990), as explained in section 2.3.3.3, was used.
Prior to inoculation of the microorganism to the production medium in the
bioreactor, the physical mass transfer coefficient (KLa0) was determined. After
inoculation of the microorganism to the bioreactor, the dynamic oxygen transfer
experiments were carried out at certain cultivation times for a short period of
time, so that the biological activities of the microorganisms are unaffected.
During this period, while the air inlet was totally ceased, the agitation rate was
lowered to N=100 min-1 in order to lower the effect of surface aeration (Çelik,
2003).
3.7 Mass Flux Balance-Based Analysis
Effects of the oxygen transfer conditions on the intracellular carbon flux
distributions were investigated by the metabolic flux analysis. The reaction
network of Bacillus licheniformis given in Appendix G represented by the
metabolic system sums up to a total of 105 metabolites and 149 reaction fluxes.
The optimized program GAMS 2.25 (General Algebraic Modeling System, GAMS
Development Corp., Washington, DC) was used to solve mass-flux balance
equation (Eq 2.20) given in Section 2.4. Using the mathematical programming,
optimum flux distributions were obtained by minimizing the objective function Z
(Eq 2.21). The model variables that are the reaction fluxes of metabolites were
expressed in mmol g-1 DW h-1; and the flux towards biomass represented the
specific growth rate, µ in h-1 (Çalık, 1998).
44
CHAPTER 4
RESULTS AND DISCUSSION
This study focuses on the effects of oxygen transfer on β-lactamase
production by Bacillus licheniformis on a defined medium. In order to clarify the
oxygen transfer effects on the production of β-lactamase, firstly a glucose based
defined medium was designed and using this medium, the effects of bioreactor
operation parameters, i.e., pH and temperature, on β-lactamase activity and cell
formation were investigated in laboratory scale bioreactors. Thereafter, using the
optimized medium the effects of oxygen transfer on cell generation, substrate
consumption, product (β-lactamase) and by-products formation were
investigated in the pilot scale bioreactor. Finally, the influence of oxygen transfer
conditions on the intracellular reaction rates in β-lactamase production by
B.licheniformis under well-defined batch bioreactor conditions was investigated
using metabolic flux analysis to evaluate the effects of oxygen on the
metabolism.
4.1 Medium Design
In order to design a defined medium firstly yeast extract was omitted from
the medium found in the study of Çalık and Çelik (2004), and medium, that
contained (kg m-3): glucose, 8; (NH4)2HPO4, 4.7 and the salt solution in which
the β-lactamase activity was obtained as 60 U cm-3 was considered as the
starting point for the medium design experiments and the medium was named
as the reference production medium (RPM).
In this context, the effects of (NH4)2HPO4 concentration was investigated
in agitation and heating rate controlled laboratory scale bioreactors as it was
found as the optimum nitrogen source in the study of Çalık and Çelik (2004).
4.1.1 Effect of Nitrogen Source Concentration
Firstly, the effect of (NH4)2HPO4 concentration on β- lactamase activity
was investigated within the range corresponding to the initial nitrogen
45
concentrations of CN0=0.0 – 4.0 kg m-3 at 37°C with an initial pH of pH0=7.2. As
can be seen from Figure 4.1 the medium containing initial nitrogen concentration
of 1.5 kg m-3 gave the maximum β-lactamase activity as A=76 U cm-3.
Furthermore, it was observed that higher nitrogen content had an inhibitory
effect on both cell formation and beta-lactamase activity.
0
20
40
60
80
0 1 2 3 4
Initial Nitrogen Concentration kg m-3
Act
ivity,
U c
m-3
Figure 4.1 The variations in β-lactamase activity with the initial nitrogen
concentration. t=32 h, V=33 cm3, T=37°C, pH0=7.2, N=200 min-1.
4.2 Bioreactor Operation Parameters
By using B.licheniformis 749/C and the medium containing 8 kg m-3
glucose, 7.1 kg m-3 (NH4)2HPO4 and the salt solution, the bioreactor operation
parameters, i.e., pH and temperature were investigated in the laboratory scale
bioreactors. Thereafter the effect of the initial glucose concentration was
investigated.
46
4.2.1 Effect of pH and Temperature
The medium design experiments were conducted with an initial pH of 7.2 in
media without buffer. Under the scope of determining the most favorable
bioreactor operation conditions, the effect of pH control was investigated first,
since some bioprocesses require controlled pH conditions, while others might
require uncontrolled pH operations (Çalık et al.,2002).
The effect of pH control was investigated in an initial pH range of 5.8-8.0,
in media with NaH2PO4 - Na2HPO4 buffer, and in media without buffer, where the
initial pH was adjusted by the addition of either 5M KOH or 10M H3PO4.
Comparing the controlled and uncontrolled-pH operations; it can be observed at
pH0= 7.2-7.6 uncontrolled-pH operation favors β-lactamase production (Figure
4.2). As seen in Figure 4.2, the highest β-lactamase activity was obtained at
pH0=7.5 uncontrolled-pH operation, the activity value (A=113 U cm-3) obtained
was approximately 1.5-fold higher than that of pH0=7.2. Çalık and Çelik (2004);
and Sargantanis and Karim (1996) stated that controlled-pH operation was not
beneficial for β-lactamase productivity.
0
20
40
60
80
100
120
5.5 6.0 6.5 7.0 7.5 8.0
pH0
Act
ivity,
U c
m-3
Figure 4.2 The variations in β-lactamase activity with the initial pH. V=33 cm3,
T=37°C, N=200 min-1, t= 32 h, w/o buffer, (∆); buffer, (□).
47
Thereafter, the effects of pH and temperature were investigated in the
medium without buffer. As seen in Figure 4.3, T=37°C, and pH0=7.5 were found
to be the most favorable conditions for β-lactamase activity. These results are
consistent with the pH and temperature range used in the literature for β-
lactamase production by Bacillus species (Sargent et al.,1968; Sargantanis and
Karim, 1996- 1998).
0
20
40
60
80
100
120
7.00 7.25 7.50 7.75 8.00pHo
Act
ivity,
U c
m-3
Figure 4.3 The variations in β-lactamase activity with the initial pH and
temperature of the cultivation medium. at t=32 h, V=33 cm3, N=200
min-1, T (°C) : 32 ,(♦); 37, ( ); 40, (▲).
4.2.2 Effect of Carbon Source Concentration
Glucose, being easily metabolized by microorganisms, is widely used in
fermentation media. The effects of glucose concentration on β-lactamase
production were investigated in the range of CG0=6.0, 7.0, 8.0, 9.0, 10.0, 11.0,
and 12.0 kg m-3, in the medium containing 7.1 kg m-3 (NH4)2HPO4 and the salt
solution at a cultivation temperature of 37°C with an initial pH of 7.5. As can be
seen in Figure 4.4 the activity of β-lactamase did not change significantly in this
range and CG°=7 kg m-3 was selected as the initial glucose concentration to be
used in the pilot-scale bioreactor experiments.
48
0
20
40
60
80
100
120
5 6 7 8 9 10 11 12 13
CG, kg m-3
Act
ivity,
U c
m-3
Figure 4.4 The variations in β-lactamase activity with the initial glucose
concentration. t=32 h, V=33 cm3, T=37°C, pH0 =7.2, N=200 min-1.
4.2.3 The Optimized Medium
As a result, among the investigated media, the highest β-lactamase activity
was obtained at T=37°C and pH0 =7.5 as 115 U cm-3, in the medium containing
7.0 kg m-3 glucose, 7.1 kg m-3 (NH4)2HPO4, and the salt solution which was 2
fold higher than the activity obtained in the RPM.
4.3 Effects of Oxygen Transfer
Using the optimized defined medium, T and pH conditions obtained in the
laboratory scale bioreactors the effects of oxygen transfer on fermentation and
oxygen transfer characteristics were investigated in the pilot scale bioreactor
system by using three agitation rates N = 250, 500, 750 min-1 and three air inlet
rates Q0/VR = 0.2, 0.5, 1 vvm. The effects of oxygen transfer were investigated
at seven different conditions with the above values of the Q0/VR and N. These
conditions were abbreviated as given in Table 4.1 according to the oxygen-
transfer conditions applied. Throughout the bioprocess, dissolved oxygen, pH,
glucose concentration, cell concentration, β-lactamase activity, amino acid and
organic acid concentrations, liquid phase mass transfer coefficient, specific rates
and yield coefficients were determined.
49
Table 4.1 Oxygen transfer conditions
# Q0/VR, vvm N, min-1 Abbreviation
1 0.2 250 LimOT
2 0.5 250 LOT1
3 0.2 500 LOT2
4 0.5 500 MOT1
5 0.2 750 MOT2
6 1.0 500 HOT1
7 0.5 750 HOT2
4.3.1 Dissolved Oxygen Concentration and pH Profiles
The variations in dissolved oxygen concentration (CO) and medium pH with
the cultivation time, air inlet rate, and agitation rate are shown in Figure 4.5 and
4.6, respectively. CO depends on the extent of the OTR to the media and the
OUR of the cells. When the OTR was very low, i.e. at LimOT and to an extent at
LOT1 conditions the CO exhibited a sudden drop at the early hours of the
fermentation and at t= 1-27 h for LimOT and, at t=2-10.5 h for LOT1 the
transferred oxygen was totally consumed. When the OTR was higher, i.e., at
LOT2, MOT1, and MOT2 conditions, a decrease and/or an increase in the dissolved
oxygen level with cultivation time was observed depending on the metabolic
stage of the growth. Further, at HOT1 and HOT2 conditions, although the biomass
concentration increased, CO did not change considerably throughout the
bioprocess as the OTR was high enough. Considering the CO profiles, Q0/VR = 0.2
vvm and N =250 min-1 (LimOT) is regarded as “limited-oxygen transfer”
condition; Q0/VR = 0.5 vvm and N =250 min-1 (LOT1), and Q0/VR = 0.2 vvm and
N =500 min-1 (LOT2) are regarded as “low-oxygen transfer” conditions; Q0/VR =
0.5 vvm and N =500 min-1 (MOT1), Q0/VR = 0.2 vvm and N =750 min-1 (MOT2)
are regarded as “medium oxygen transfer” conditions; and lastly Q0/VR = 1.0
vvm and N =500 min-1 (HOT1) and Q0/VR = 0.5 vvm and N =750 min-1 (HOT2)
are regarded as “high-oxygen transfer” condition.
The initial pH value was pH0=7.5 for all the conditions. The locus of pH
versus time profiles were similar at LOT2, MOT1, MOT2, HOT1, and HOT2
conditions, and pH has a tendency to decrease until t=10 h; thereafter, it
50
reached to the stationary phase. However, at LOT1 and LimOT conditions the
decrease rate of pH was higher than the other conditions. At LimOT condition
where the lowest pH was observed, the pH of the fermentation broth decreased
until t= 12 h; whereas, at t=12-19 h it was constant; and after t=19 h pH
increased.
0.00
0.02
0.04
0.06
0.08
0.10
0.12
0.14
0.16
0.18
0.20
0 5 10 15 20 25 30t,h
C0,
mol m
-3
Figure 4.5 The variations in dissolved oxygen concentration with cultivation
time. T=370C, C0*= 0.20 mol m-3, VR= 1.65 * 10-3 m3. LimOT: (●);
LOT1:(▲); LOT2: ( ); MOT1: (○); MOT2: (∆); HOT1: (□); HOT2: (x).
In the literature, Çelik and Çalık (2004) reported the variations in pH and
dissolved oxygen profiles throughout the β-lactamase production process at
320C, pH0 = 6.0, N=500 min-1, and Q0/VR = 0.5 vvm in the semi-defined
medium. In the above study, pH decreased until t=4.5 h to pH=5.8, thereafter it
increased and reached a constant value of pH= 7.6. The CO decreased suddenly
at the early stage of the fermentation and at t= 4.5-7 h the transferred oxygen
was totally consumed. Thereafter, the CO gradually increased. The CO profile
obtained by Çelik and Çalık (2004) and CO obtained in this work at MOT1
condition (N=500 min-1, and Q0/VR = 0.5 vvm) were similar; however, between
51
t=4.5-7 h because of the higher cell concentration obtained by Çelik and Çalık
(2004) the transferred oxygen was totally consumed; whereas, in this study the
dissolved oxygen concentration decreased until t=4 h and then increased.
5.5
6
6.5
7
7.5
0 5 10 15 20 25 30t,h
pH
Figure 4.6 The variations in medium pH with cultivation time. CG0 = 7.0 kg m-3,
T=370C, VR= 1.65 * 10-3 m3. LimOT: (●); LOT1:(▲); LOT2: ( ); MOT1:
(○); MOT2: (∆); HOT1: (□); HOT2: (x).
4.3.2 Glucose Concentration Profiles
Variations in the glucose concentration with the cultivation time, air inlet
rate, and agitation rate are given in Figure 4.7. Glucose concentration (CG0 = 7.0
kg m-3), decreased with the cultivation time, as expected. At the end of the
bioprocesses, the lowest amount of glucose was attained at LimOT and MOT1
conditions that correspond to the consumption of %91.5 of the initial glucose.
However the rate of glucose consumption was the highest:
1. at t=0-2 h at LOT1 condition,
2. at t= 2-5 h at LimOT condition;
52
3. at t= 5-11 h at HOT2 condition;
4. at t= 11-20 h at LOT2 condition;
5. at t= 20-28 h at MOT1 condition.
0
1
2
3
4
5
6
7
0 5 10 15 20 25 30t,h
CG,
kg m
-3
Figure 4.7 The variations in glucose concentration with cultivation time.
CG0=7.0 kg m-3, T=37°C, VR= 1.65 * 10-3 m3. LimOT: (●); LOT1:(▲);
LOT2: ( ); MOT1: (○); MOT2: (∆); HOT1: (□); HOT2: (x).
4.3.3 Cell Concentration Profiles
The variations in the cell concentration with cultivation time and the
oxygen transfer conditions applied are given in Figure 4.8. Cell concentration
increased at a high rate between t=2-7 h, and then reached the stationary
phase. The highest cell concentrations were obtained at MOT2 and HOT2
conditions as CX= 0.67 kg m-3 and the lowest cell concentration was obtained at
LimOT and HOT1 as CX= 0.54 kg m-3.
53
0
0.1
0.2
0.3
0.4
0.5
0.6
0.7
0.8
0 1 2 3 4 5 6 7 8 9 10 11 12t,h
Cx,
kg m
-3
Figure 4.8 The variations in cell concentration with cultivation time. CG0=7.0 kg
m-3 T=37°C, VR= 1.65 * 10-3 m3. LimOT: (●); LOT1:(▲); LOT2: ( );
MOT1: (○); MOT2: (∆); HOT1: (□); HOT2: (x).
4.3.4 Beta-lactamase Activity Profiles
The variations in β-lactamase activity with the cultivation time, air inlet rate
and agitation rate are given in Figure 4.9. As can be seen from Figure 4.9 the
lowest β-lactamase activity was obtained at LimOT condition where the lowest
cell concentration was obtained. At MOT1 condition β-lactamase activity was
higher than the other conditions throughout the process but at t=24 h LOT2 and
MOT1 gave all most the same β-lactamase activity values ca. A=90 U cm-3. In
the process the cultivation time in which the highest β-lactamase activity was
obtained shifted 1.33-fold to an earlier cultivation time (t=24h) compared to the
laboratory scale experiments (t=32h) with a cost of 22 % lower activity.
54
0
20
40
60
80
100
0 5 10 15 20 25 30t,h
A,
U c
m-3
Figure 4.9 The variations in β-lactamase activity with cultivation time. CG0=7.0
kg m-3, T=37°C, VR= 1.65 * 10-3 m3. LimOT: (●); LOT1:(▲); LOT2: ( );
MOT1: (○); MOT2: (∆); HOT1: (□); HOT2: (x).
4.3.5 Amino Acid Concentrations
The oxygen transfer conditions influenced the amino acids synthesis and
their concentrations in the fermentation broth, as the synthesis of some of them
might be the rate limiting step(s) in the metabolic reaction network in β-
lactamase synthesis. For the production of proteins, regulation of the metabolic
reaction network should cause good coupling of supply and demand for the
amino acids (Çalık et al., 2000).
The variations in amino acid concentrations in the fermentation broth
with cultivation time and for seven different oxygen transfer conditions applied
were given in Table 4.2.a, 4.2.b, 4.2.c, 4.2.d, 4.2.e, 4.2.f, 4.2.g. At all the
oxygen transfer conditions, generally aspartic acid and the asparagine were the
amino acids detected in the broth.
At LimOT condition all the amino acids but glutamic acid, histidine,
proline, tyrosine, valine, methionine, cystein, isoleucine and lysine were present
55
in the fermentation broth. Nevertheless, at LOT1 condition besides these amino
acids; phenlylalanine was not present in the fermentation broth; while at LOT2
condition arginine, threonine, alanine, valine, methionine, cystein, ornithine,
tyrptophan and lysine were not detected in the fermentation broth. At MOT1
condition glutamic acid, threonine, alanine, tyrosine, isoleucine, leucine and
lysine; at MOT2 condition glutamic acid, glycine, threonine, alanine, tyrosine,
ornithine, tyrptophan and lysine; at HOT1 condition glutamic acid, threonine,
alanine, tyrosine, isoleucine, leucine and lysine and lastly at HOT2 condition
glutamic acid, tyrosine, valine, methionine, cystein isoleucine and lysine were
not present in the fermentation broth. In general the amino acid concentrations
in the fermentation broth was low and considering all the amino acid profiles and
oxygen transfer conditions, arginine concentration was the highest at LimOT
condition obtained as 0.072 kg m-3 at t=3 h.
As it is seen from the Table 4.2.a, 4.2.b, 4.2.c, 4.2.d, 4.2.e, 4.2.f, and
4.2.g the total amino acid concentration excreted to the fermentation broth was
maximum at LOT2 condition at t=24 h as TAA = 0.133 kg m-3 and minimum at
HOT1 condition at t=20 h as TAA = 0.001 kg m-3. At LimOT condition (Table
4.2.a) total amino acid concentration decreased sharply between t=3-5 h and
then it was almost constant throughout the fermentation at 0.010 kg m-3,
nevertheless at LOT1 condition (Table 4.2.b) it increased between t=3-11 and
gave a maximum at t=11 h and then decreased until t=20 h and reached a
constant value between t= 20-24 h. At MOT1 condition (Table 4.2.c) total amino
acid concentration decreased between t=3-11 h and then increased and gave a
maximum at t= 20 h. In general at HOT1 and HOT2 conditions total amino acid
concentrations were less than the other conditions and these conditions showed
similar profiles that is, total amino acid concentration decreased between t=3-20
h and then showed a little increase between t= 20-24 h.
56
Table 4.2.a The variations in amino acid concentrations in the fermentation
broth with the cultivation time at LimOT condition.
Cultivation time, h
CAA, kg m-3 3 5 11 20 24
Asn 0.003 0.002 0.003 0.004
Asp 0.004 0.007
Gln 0.001
Ser 0.002
Gly 0.006 0.003
Arg 0.072
Thr 0.003
Ala 0.003
Leu 0.003 0.003 0.003 0.003
Phe 0.007
Trp 0.007
Total 0.101 0.007 0.005 0.012 0.014
Table 4.2.b The variations in amino acid concentrations in the fermentation
broth with the cultivation time at LOT1 condition.
Cultivation time, h
CAA, kg m-3 3 5 11 20 24
Asn 0.001 0.002 0.002 0.002 0.010
Asp 0.001 0.005 0.002 0.007
Gln 0.001 0.003 0.002 0.001
Ser 0.001 0.002 0.002
Gly 0.003 0.001 0.006 0.003
His
Arg 0.014
Thr 0.001 0.010
Ala 0.009
Leu 0.004 0.006 0.007 0.006 0.006
Phe
Trp 0.028 0.010 0.003
Total 0.009 0.040 0.068 0.020 0.024
57
Table 4.2.c The variations in amino acid concentrations in the fermentation
broth with the cultivation time at LOT2 condition.
Cultivation time, h
CAA, kg m-3 3 5 11 20 24
Asn 0.003 0.006 0.006
Asp 0.003 0.006 0.006 0.022
Glu 0.007 0.013
Gln 0.003
Ser 0.002
Gly 0.002 0.003
His 0.034
Pro 0.004 0.011
Tyr 0.006
Ile 0.004 0.023
Leu 0.003 0.005 0.010
Phe 0.003 0.003
Total 0.006 0.012 0.009 0.028 0.133
Table 4.2.d The variations in amino acid concentrations in the fermentation
broth with the cultivation time at MOT1 condition.
Cultivation time, h
CAA, kg m-3 3 5 11 20 24
Asn 0.009 0.002 0.001 0.003 0.002
Asp 0.003 0.002 0.003 0.025 0.004
Gln 0.001
Ser 0.001 0.001 0.001 0.001
Gly 0.001 0.001 0.001
His 0.008 0.003
Arg 0.008
Pro 0.007 0.018
Val 0.003 0.003 0.003 0.005 0.003
Met 0.002 0.003 0.003 0.005 0.003
Cys 0.002 0.003 0.002 0.006 0.002
Phe 0.005 0.006 0.004
Trp 0.002 0.001
Total 0.035 0.030 0.022 0.066 0..019
58
Table 4.2.e The variations in amino acid concentrations in the fermentation
broth with the cultivation time at MOT2 condition.
Cultivation time, h
CAA, kg m-3 3 5 11 20 24
Asn 0.008 0.004 0.004
Asp 0.005
Gln 0.001
His 0.017 0.008
Arg 0.028
Pro 0.003 0.003
Val 0.006 0.001
Met 0.006
Cys 0.001
Leu 0.004 0.002 0.003
Phe 0.004
Total 0.041 0.046 0.002 0.009 0.010
Table 4.2.f The variations in amino acid concentrations in the fermentation
broth with the cultivation time at HOT1 condition.
Cultivation time, h
CAA, kg m-3 3 5 11 20 24
Asn 0.005 0.002 0.007
Asp 0.012
Gly 0.001 0.002
His 0.003
Arg 0.018
Thr 0.003 0.001
Ala 0.004 0.001
Pro 0.006
Ile 0.001 0.002
Leu 0.001
Phe 0.001 0.002 0.001 0.002
Total 0.031 0.020 0.011 0.001 0.012
59
Table 4.2.g The variations in amino acid concentrations in the fermentation
broth with the cultivation time at HOT2 condition.
Cultivation time, h
CAA, kg m-3 3 5 11 20 24
Asn 0.002 0.001 0.001 0.003 0.003
Asp 0.002 0.003 0.002
Gln 0.001
Gly 0.005 0.002
His 0.001
Arg
Thr 0.002 0.001
Ala 0.001
Leu 0.007 0.007 0.008 0.007
Phe 0.004
Trp 0.006 0.002 0.002
Total 0.028 0.011 0.011 0.006 0.017
4.3.6 Organic Acid Concentrations
Since oxygen acts as the driving force in the TCA cycle and the rate of the
TCA cycle is influenced by the oxygen transfer conditions in the metabolic
reaction network (Çalık et al., 2000), the synthesis of the TCA cycle organic
acids, acetic acid and lactic acid are important for increasing the yield and the
selectivity. At all the oxygen transfer conditions, generally acetic acid and lactic
acid are the organic acids detected in the broth at high concentrations. The
variations of organic acid concentrations with the cultivation time and oxygen-
transfer conditions are shown in Table 4.3. At LimOT condition, at t=3, 5, 11, 20
h, the organic acid having the highest concentration was lactic acid in contrast to
the other oxygen transfer conditions applied, as at all the others acetic acid was
the main organic acid excreted to the fermentation broth. At LimOT condition at
t=11 h lactic acid was excreted having the concentration of 1.464 kg m-3 which
was the highest value obtained throughout the bioprocesses.
60
Table 4.3 The variations in organic acid concentrations in the fermentation
broth with the cultivation time at LimOT, LOT1, LOT2 MOT1, MOT2,
HOT1, and HOT2 conditions.
Condition T
(h) COA, kg m-3
Cit αKG Suc Ac Lac But Gluc
3 0.267 0.325
5 0.507 1.112 0.003
11 0.009 0.020 0.344 1.464
20 0.176 0.899 1.436 0.002 LimOT
24 1.290 0.968
3 0.391 0.185
5 0.664 0.667 0.002
11 0.007 0.987 0.636
20 0.013 0.577 0.386
LOT1
24 0.007 0.362 0.218
3 0.339 0.041
5 0.620 0.035
11 0.667 0.012
20 0.405 LOT2
24 0.241
3 0.432 0.010 0.006
5 0.553 0.017 0.009
11 0.016 0.550 0.020 0.023
20 0.675 0.061 0.019 MOT1
24 0.392 0.043 0.006
3 0.607
5 0.858 0.006
11 1.248
20 0.548 0.002 MOT2
24 0.508 0.025
3 0.642 0.006
5 0.647 0.001
11 1.254 0.019
20 0.811 0.011 HOT1
24 0.592 0.029
3 0.616 0.049 0.030
5 0.719 0.009 0.004
11 0.688 0.017
20 0.664 0.046 0.021 HOT2
24 0.324 0.028
61
The variations in total organic acid concentration with the cultivation time
and the oxygen transfer conditions are given in Figure 4.10. As it is seen in the
figure, the total organic acid concentration excreted to the fermentation broth
was maximum at LimOT condition at t=20 h as TOA = 2.513 kg m-3, explaining
the reason of the highest rate of decrease in the medium pH at these condition
and minimum at HOT2 condition at t=24 h as TOA = 0.352 kg m-3. Total organic
acid concentrations as well as the non-detected organic acids can be seen in
Table 4.4. As it is clear in Table 4.4 at LOT2, MOT1, MOT2, HOT1 and HOT2
conditions, the TCA cycle organic acids α-ketoglutaric acid and succinic acid were
not detected in the fermentation broth. Nevertheless, under LimOT condition α-
ketoglutaric and succinic acids and under LOT1 condition succinic acid were
excreted to the fermentation broth. Under the lower range of oxygen transfer
conditions, LimOT and LOT1, due to the insufficient operation of TCA cycle α-
ketoglutaric and succinic acids were excreted to the fermentation broth.
0.0
0.5
1.0
1.5
2.0
2.5
0 5 10 15 20 25t,h
TO
A,
kg m
-3
Figure 4.10 The variations in total organic acid concentration with cultivation
time. CG0=7.0 kg m-3, T=37°C, VR= 1.65 * 10-3 m3. LimOT: (●);
LOT1:(▲); LOT2: ( ); MOT1: (○); MOT2: (∆); HOT1: (□); HOT2: (x).
62
Table 4.4 The variations of total organic acid concentration and non-excreted
organic acids with the constant air inlet and agitation rates.
Oxygen-transfer
condition
TOA (kg m-3)
Non-excreted organic acids
LimOT 0.592-2.513 citric, pyruvic, gluconic acids
LOT1 0.576-1.630 citric, pyruvic, α-KG, gluconic acids
LOT2 0.268-0.679 citric, pyruvic, α-KG, gluconic, succinic acids
MOT1 0.441-0.755 pyruvic, α-KG, succinic acids
MOT2 0.533-1.248 citric, pyruvic, α-KG, lactic, succinic acids
HOT1 0.621-1.273 citric, pyruvic, α-KG, lactic, succinic acids
HOT2 0.352-0.732 citric, pyruvic, α-KG, succinic acids
4.3.7 Oxygen Transfer Characteristics
In β-lactamase production by Bacillus licheniformis in a defined medium,
the Dynamic Method was applied to find the oxygen transfer parameters, i.e.,
oxygen uptake rate (OUR), r0, and oxygen transfer coefficient, KLa, during the
cultivation times corresponding to the characteristic regions of the batch
bioprocess, for different oxygen transfer conditions applied. At t<0 h, the
physical oxygen transfer coefficient KLao was measured in the medium in the
absence of the microorganism. The variations in KLa, oxygen uptake rate,
oxygen transfer rate and the enhancement factor E (=KLa/KLao) throughout the
bioprocess are given in Table 4.5.a and 4.5.b. As dissolved oxygen concentration
in the medium was very low between t=1-27 h at LimOT, between t=2-11 h at
LOT1, between t=1-8 h at LOT2 conditions, the Dynamic Method could not be
applied. For LimOT, LOT1, and LOT2 conditions the following assumption was
used :
* E=1 and KLa0=KLa,
to calculate the OTR. When mass transfer is accompanied by a chemical
reaction, enhancement factor can be enhanced several-fold depending on the
relative rates of mass transfer and chemical reaction; therefore, obtained OTR
values can be considered as the lowest OTR values.
63
4.3.7.1 Volumetric Oxygen Transfer Coefficient
As can be seen from Table 4.5.a and Table 4.5.b, throughout the
bioprocess in general KLa increased and then decreased at MOT1 and MOT2
conditions; however, at LOT1, LOT2, HOT1, and HOT2 it gradually increased with
the residence time. KLa depends on agitation rate, temperature, rheological
properties of the fermentation medium, and presence of fine particles in the
mass transfer zone. Since temperature and agitation rate were kept constant
throughout the bioprocess, the reason for the change in KLa could be the change
in the viscosity of the medium due to the secreted metabolites and growth.
Average KLa value increased with the increase in the agitation and aeration
rates as expected and when compared with the gas flow rate, the agitation rate
was a more effective parameter for increasing the oxygen transfer coefficient.
The highest oxygen transfer coefficient was obtained at HOT2 condition as 0.044
s-1 at t=2 and t=20 h of the cultivation time.
In general the enhancement factors E were slightly higher than 1.0,
showing that a slow reaction is accompanied by mass transfer as expected in
most of the fermentation processes accomplished in stirred bioreactors and they
did not show a significant difference at oxygen transfer conditions applied and
changed in the range E= 1.0-2.1.
The KLa values were also calculated from the correlations (Eq 4.1) with
the corresponding constants given in Table 2.5. The variations in oxygen transfer
coefficients obtained from correlations with the average experimental values are
given in Table 4.6. There is a fairly good agreement between the experimental
and correlated values for coelescing bubbles (Eq 1-4) given by Moo-Young and
Blanch (1981), within the agitation and air-inlet rate range used. Average
experimental values were used for comparison because of the dynamic behavior
of the fermentation media, which could not be correlated for the entire
fermentation process.
αβ
sR
GL V
VP
kaK
= (4.1)
64
In the calculations, the power input PG in aerated stirred liquid was
calculated from the following correlation (Rose, 1981):
AeFrDDPP DDIG
I /95.1115.038.4 Re)/(192)/log( −= (4.2)
The power input in gas free stirred liquid was calculated from the Equation
4.5 given below (Nielsen and Villadsen, 1994):
53Ilp DNNP ρ= (4.3)
The power number was obtained from Reynolds number versus Power
number graph given in Figure 4.11 (Nielsen and Villadsen, 1994).
Figure 4.11 Correlation between the power number and the reynolds number
for a bioreactor system with one-six bladed Rushton turbine impeller
and baffles.
65
4.3.7.2 Oxygen Uptake Rate
Increase in substrate consumption rate, cell concentration, and cell
production rate, increased the oxygen uptake rate (OUR), which depends on the
metabolic functions of the cell.
As expected, at the early stage of the fermentation OUR tend to increase at
all conditions, mainly as a result of increase in the cell production rate, the cell
concentration and the substrate consumption rates. Generally, after t=11 h as
the biomass production rate decreased, OUR also decreased. The highest OUR
was observed at LOT2 condition at t=5 h as 1.6*10-3 mol m-3s-1.
In order to compare mass transfer and biochemical reaction rates in the β-
lactamase production process by B. licheniformis which was investigated under
seven different constant oxygen transfer conditions, the maximum possible
oxygen utilization rate (OD=µmaxCX/YX/O) and the maximum possible mass
transfer rate (OTRmax=KLaCO*) were calculated throughout the bioprocess. A kind
of Damköhler number, Da, defined as maximum possible oxygen utilization rate
per maximum mass transfer rate (Çalık et al., 2000 and 2003); and
effectiveness factor, η, defined as the oxygen uptake rate per maximum possible
oxygen utilization rate values (Çalık et al., 2000 and 2003) can be seen in Table
4.5.a and 4.5.b.
It is clear in Table 4.5.a that, LimOT, LOT1 and LOT2 conditions, were
mass-transfer limited conditions (Da>>1). While, at MOT1, MOT2, HOT1, and
HOT2 conditions, at=2-8 h the mass-transfer resistance was more effective
(Da>>1).
As it is apparent from Table 4.5.a and Table 4.5.b, the high effectiveness
factor, η, values until t=5 h indicate that the cells are consuming oxygen with
such a high rate that maximum possible oxygen utilization (OD) value is
approached and thereafter the decrease in η indicates that the cells are
consuming lower oxygen than the oxygen demand (OD).
66
η
OU
R/O
D
0.3
36
0.1
73
0.0
18
0.3
61
0.0
80
0.6
56
0.0
49
0.0
16
Da
OD
/OTR
max
2.9
32
5.7
65
55.3
18
2.7
37
12.2
93
0.9
91
16.3
63
31.7
20
O
D*10
3
(mol m
-3s-1
)
4.1
05
8.0
71
77.4
45
4.3
80
19.6
68
1.9
83
32.7
25
63.4
40
O
UR*10
3
(mol m
-3s-1
)
1.3
79
1.3
93
1.3
79
1.3
86
1.3
93
1.3
86
1.4
00
1.5
76
1.5
76
1.5
76
1.1
39
0.5
00
0.5
00
0.4
00
1.3
00
1.6
00
1.0
00
1.0
00
0.8
00
0.7
00
0.7
00
O
TR
max
*10
3
(mol m
-3s-1
)
1.4
00
1.4
00
1.4
00
1.4
00
1.4
00
1.4
00
1.4
00
1.6
00
1.6
00
1.6
00
1.6
00
2.8
40
2.8
00
3.3
20
2.0
00
2.0
00
2.0
00
2.6
00
2.8
20
3.2
60
4.2
00
O
TR*10
3
(mol m
-3s-1
)
1.3
79
1.3
93
1.3
79
1.3
86
1.3
93
1.3
86
1.4
00
1.5
76
1.5
76
1.5
76
1.1
39
1.7
89
1.8
00
1.5
94
1.2
20
1.5
96
1.0
92
1.0
43
0.9
48
0.9
19
1.2
18
E
KLa
/KLa
0
1.0
00
1.0
00
1.0
00
1.0
00
1.0
00
1.0
00
1.0
00
1.0
00
1.0
00
1.0
00
1.0
00
1.7
75
1.7
50
2.0
75
1.0
00
1.0
00
1.0
00
1.3
00
1.4
10
1.6
30
2.1
00
K
La
(s-1
)
0.0
07
0.0
07
0.0
07
0.0
07
0.0
07
0.0
07
0.0
07
0.0
08
0.0
08
0.0
08
0.0
08
0.0
14
0.0
14
0.0
17
0.0
10
0.0
10
0.0
10
0.0
13
0.0
14
0.0
16
0.0
21
t (h)
2*
5*
8*
11*
20*
24*
28*
2*
5*
8*
11*
20
24
28
2*
5*
8*
11
20
24
28
Tab
le 4
.5.a
The
variat
ions
in o
xygen
tra
nsf
er p
aram
eter
s w
ith c
ultiv
atio
n t
ime
at L
imO
T.
LOT
1 a
nd L
OT
2 c
onditio
ns
Conditio
n
LIM
OT
LOT
1
LOT
2
67
η
OU
R/O
D
0.4
65
0.0
60
0.4
12
0.1
25
0.6
07
0.1
25
0.0
52
0.9
62
0.0
33
Da
OD
/OTR
max
0.6
12
5.1
42
0.6
07
2.7
14
0.4
77
1.6
79
3.5
12
0.1
17
5.1
70
OD
*10
3
(mol m
-3s-1
) 1.9
34
18.3
04
2.4
27
12.0
34
1.8
11
6.3
79
13.3
47
1.0
40
36.1
92
OU
R*10
3
(mol m
-3s-1
) 0.9
00
1.1
00
1.0
00
0.9
00
0.9
00
0.9
00
0.9
00
1.0
00
1.5
00
1.3
00
1.2
00
1.0
00
0.8
00
0.8
00
1.1
00
0.8
00
0.7
00
0.6
00
0.6
00
0.6
00
0.6
00
1.0
00
1.2
00
0.9
00
0.9
00
0.9
00
OTRm
ax*10
3
(mol m
-3s-1
) 3.1
60
3.5
60
5.2
40
5.2
40
4.0
00
4.4
00
4.4
00
4.0
00
4.4
34
4.6
00
4.7
80
4.7
20
6.6
00
5.5
00
3.8
00
3.8
00
3.8
00
3.8
00
4.0
00
5.8
00
7.2
00
8.8
60
7.0
00
6.0
40
5.8
00
8.8
00
OTR*10
3
(mol m
-3s-1
) 1.0
55
1.8
08
1.9
96
1.4
83
1.1
12
1.1
62
1.2
14
0.7
52
1.3
30
2.0
70
1.2
43
1.0
38
0.9
04
0.7
98
0.7
60
1.0
28
1.0
11
1.0
48
0.3
52
0.8
29
0.9
36
0.7
53
0.2
94
1.0
45
0.6
38
1.0
21
E
KLa
/KLa
0
1.0
90
1.2
28
1.8
07
1.8
07
1.3
79
1.5
17
1.5
17
1.0
58
1.1
73
1.2
17
1.2
65
1.2
49
1.7
46
1.4
55
1.0
00
1.0
00
1.0
00
1.0
00
1.0
53
1.5
26
1.8
95
1.7
58
1.3
89
1.1
98
1.1
51
1.7
46
KLa
(s
-1)
0.0
16
0.0
18
0.0
26
0.0
26
0.0
20
0.0
22
0.0
22
0.0
20
0.0
22
0.0
23
0.0
24
0.0
24
0.0
33
0.0
28
0.0
19
0.0
19
0.0
19
0.0
19
0.0
20
0.0
29
0.0
36
0.0
44
0.0
35
0.0
30
0.0
29
0.0
44
t (h)
2
5
8
11
20
24
28
2
5
8
11
20
24
28
2
5
8
11
20
24
28
2
5
8
11
20
Tab
le 4
.5.b
The
variat
ions
in o
xygen
tra
nsf
er p
ara
met
ers
with t
he
cultiv
ation t
ime
at M
OT
1.
MO
T2.
HO
T1 a
nd H
OT
2 c
onditio
ns.
Conditio
n
MO
T1
MO
T2
HO
T1
HO
T2
68
Eq 8
0.0
46
0.0
53
0.1
94
0.2
15
0.2
15
0.4
44
0.4
75
Eq 7
0.0
12
0.0
16
0.0
31
0.0
42
0.0
54
0.0
50
0.0
72
Eq 6
0.0
18
0.0
20
0.0
74
0.0
82
0.1
69
0.0
82
0.1
81
Eq 5
0.0
07
0.0
09
0.0
31
0.0
38
0.0
71
0.0
40
0.0
83
Eq 4
0.0
05
0.0
07
0.0
11
0.0
16
0.0
17
0.0
21
0.0
25
Eq 3
0.0
06
0.0
08
0.0
15
0.0
21
0.0
27
0.0
25
0.0
36
Eq 2
0.0
05
0.0
07
0.0
18
0.0
24
0.0
36
0.0
29
0.0
48
Eq 1
0.0
05
0.0
07
0.0
10
0.0
16
0.0
17
0.0
20
0.0
24
KLa.
s-1
Exp
0.0
07
0.0
11
0.0
16
0.0
21
0.0
25
0.0
23
0.0
36
Tab
le 4
.6 T
he
variat
ions
in o
xygen
tra
nsf
er c
oef
fici
ents
obta
ined
fro
m d
iffe
rent
corr
elat
ions
and t
he
aver
age
exper
imen
tal va
lue.
Co
nd
itio
ns
Lim
OT
LO
T1
LO
T2
MO
T1
MO
T2
HO
T1
HO
T2
69
4.3.8 Specific Rates and Yield Coefficients
The variations in the specific growth rate, µ, the specific oxygen uptake
rate, qo, the specific substrate consumption rate, qs, the specific product
formation rate, qP, and the yield coefficients with cultivation time are given in
Table 4.7.a and 4.7.b. The variations in the specific growth rate with the
cultivation time are given in Figure 4.12 and as can be seen from the figure at all
the oxygen transfer conditions applied the specific growth rates decreased in the
logarithmic growth phase, and in general at t=7 h µ=0 h-1. The maximum
specific growth rate of µmax=1.04 h-1 was obtained at t=1 h at LOT1 condition.
The variations in specific substrate consumption, specific oxygen uptake and
specific β-lactamase production rates with cultivation time are given in Figures
4.13. 4.14 and 4.15 respectively. As seen in Figure 4.13, the specific substrate
consumption rates first decreased and then increased at all the conditions
except, LimOT and HOT1 at which they gradually decreased throughout the
fermentation. The highest value of qS was obtained at t=2 h of LOT1 condition as
2.17 kg kg-1 h-1; where the lowest value was obtained at t=28 h of LimOT and
HOT1 conditions as 0.07 kg kg-1 h-1. However, the specific oxygen uptake rates
decreased throughout the bioprocess due to the increased cell concentration and
gave a maximum at LimOT condition at t=2 h as q0=0.94 kg kg-1 h-1 and a
minimum at LOT1 condition at t=28 h as q0=0.08 kg kg-1 h-1. As can be seen in
Figure 4.15, in the β-lactamase formation the specific production rate decreased
throughout the process at all the oxygen transfer conditions applied but at
LimOT and LOT1 conditions after t=20 h the specific production rate again began
to increase. The highest value of qp was obtained at t=0.5 h at LOT2 condition as
69.5*106 U kg-1 h-1.
The yield of cell on substrate and the yield of cell on oxygen decreased with
the cultivation time at all the oxygen transfer conditions applied, however at
LimOT condition they increased between t=2-5 h. The highest YX/S value was
obtained at MOT1 condition at t=2 h as YX/S=0.72 kg kg-1 and the yield of cell on
oxygen reached a maximum, YX/O=1.49 kg kg-1, at t=2 h at MOT1 condition.
Nevertheless, the yield of substrate on oxygen showed a decrease and/or an
increase throughout the fermentation and gave the highest value at HOT2
condition at t=20 h as YS/O=8.07 kg kg-1.
70
0.0
0.2
0.4
0.6
0.8
1.0
1.2
0 2 4 6 8 10 12t,h
µ,
h-1
Figure 4.12 The variations in the specific growth rate with the cultivation time.
CG0=7.0 kg m-3, T=37°C, VR= 1.65 * 10-3 m3. LimOT: (●); LOT1:(▲);
LOT2: ( ); MOT1: (○); MOT2: (∆); HOT1: (□); HOT2: (x).
0.0
0.5
1.0
1.5
2.0
2.5
0 5 10 15 20 25 30t,h
qs,
kg k
g-1 h
-1
Figure 4.13 The variations in the specific substrate consumption rate with the
cultivation time. CG0=7.0 kg m-3, T=37°C, VR= 1.65 * 10-3 m3. LimOT:
(●); LOT1:(▲); LOT2: ( ); MOT1: (○); MOT2: (∆); HOT1: (□); HOT2: (x).
71
0.0
0.2
0.4
0.6
0.8
1.0
1.2
0 5 10 15 20 25 30t,h
q0,
kg k
g-1 h
-1
Figure 4.14 The variations in the specific oxygen uptake rate with the
cultivation time. CG0=7.0 kg m-3, T=37°C, VR= 1.65 * 10-3 m3, LimOT:
(●); LOT1:(▲); LOT2: ( ); MOT1: (○); MOT2: (∆); HOT1: (□); HOT2: (x).
-10.0
0.0
10.0
20.0
30.0
40.0
50.0
60.0
70.0
0 5 10 15 20 25 30t,h
qp,
U*10
-6 k
g-1 h
-1
Figure 4.15 The variations in the specific β-lactamase production rate with the
cultivation time. CG0=7.0 kg m-3, T=37°C, VR= 1.65 * 10-3 m3. LimOT:
(●); LOT1:(▲); LOT2: ( ); MOT1: (○); MOT2: (∆); HOT1: (□); HOT2: (x).
72
Y
s/o
(kg k
g-1
) 2.1
7
2.2
4
2.1
7
2.0
3
1.0
5
0.3
0
0.2
4
2.8
9
1.9
2
1.2
3
0.9
1
1.2
0
2.5
0
5.3
8
1.9
4
1.4
5
1.9
0
1.5
5
1.8
7
3.6
2
6.5
4
Y
x/s
(kg k
g-1
) 0.1
7
0.2
1
0.0
3
0.0
0
0.0
0
0.0
0
0.0
0
0.1
8
0.1
1
0.0
0
0.0
0
0.0
0
0.0
0
0.0
0
0.4
9
0.1
1
0.0
5
0.0
0
0.0
0
0.0
0
0.0
0
Y
x/o
(kg k
g-1
) 0.3
6
0.4
6
0.0
7
0.0
0
0.0
0
0.0
0
0.0
0
0.5
2
0.2
1
0.0
0
0.0
0
0.0
0
0.0
0
0.0
0
0.9
5
0.1
6
0.1
0
0.0
0
0.0
0
0.0
0
0.0
0
q
P*10
-6
(U k
g-1 h
-1)
7.4
7
2.1
9
1.0
4
0.6
8
0.6
9
1.2
1
2.0
4
12.7
5.7
9
4.3
2
4.1
6
4.6
3
5.3
1
6.2
8
20.3
6
7.4
7
6.5
2
5.8
6
3.9
0
2.8
7
1.7
5
qs
(kg k
g-1
h-1
) 2.0
4
0.9
2
0.6
5
0.6
0
0.3
1
0.0
9
0.0
7
2.1
7
0.7
3
0.3
7
0.2
0
0.1
2
0.2
5
0.4
3
1.3
2
0.4
5
0.3
8
0.3
1
0.2
8
0.4
7
0.8
5
q0
(kg k
g-1
h-1
) 0.9
4
0.4
1
0.3
0
0.3
0
0.3
0
0.3
0
0.3
0
0.7
5
0.3
8
0.3
0
0.2
2
0.1
0
0.1
0
0.0
8
0.6
8
0.3
1
0.2
0
0.2
0
0.1
5
0.1
3
0.1
3
r o
(kg O
2
m-3
h-1
) 0.1
6
0.1
6
0.1
6
0.1
6
0.1
6
0.1
6
0.1
6
0.1
8
0.1
8
0.1
8
0.1
3
0.0
6
0.0
6
0.0
5
0.1
5
0.1
8
0.1
2
0.1
2
0.0
9
0.0
8
0.0
8
µ
(h-1
) 0.3
4
0.1
9
0.0
2
0.0
0
0.0
0
0.0
0
0.0
0
0.3
9
0.0
8
0.0
0
0.0
0
0.0
0
0.0
0
0.0
0
0.6
5
0.0
5
0.0
2
0.0
0
0.0
0
0.0
0
0.0
0
Cx
(kg m
-3)
0.1
7
0.3
9
0.5
4
0.5
4
0.5
4
0.5
4
0.5
4
0.2
4
0.4
8
0.6
0
0.6
0
0.6
0
0.6
0
0.6
0
0.2
2
0.5
9
0.6
1
0.6
1
0.6
1
0.6
1
0.6
1
t (h)
2
5
8
11
20
24
28
2
5
8
11
20
24
28
2
5
8
11
20
24
28
Tab
le 4
.7.a
The
variat
ions
in t
he
spec
ific
rat
es a
nd y
ield
coef
fici
ents
with t
he
cultiv
atio
n t
ime
at L
imO
T.
LOT
1 a
nd L
OT
2 c
onditio
n.
Conditio
n
Lim
OT
LOT
1
LOT
2
73
Y
s/o
(kg k
g-1)
2.0
8
2.1
7
0.8
5
0.7
7
1.0
2
5.7
6
5.6
3
3.1
4
1.8
1
1.6
4
1.3
3
0.7
8
0.9
2
1.0
8
2.7
1
3.2
0
2.9
3
2.7
7
1.2
3
0.8
5
0.5
4
2.9
4
2.2
9
3.8
0
6.6
7
8.0
7
Y
x/s
(kg k
g-1)
0.7
2
0.1
6
0.0
0
0.0
0
0.0
0
0.0
0
0.0
0
0.3
3
0.2
3
0.0
0
0.0
0
0.0
0
0.0
0
0.0
0
0.3
4
0.1
9
0.1
1
0.0
0
0.0
0
0.0
0
0.0
0
0.4
2
0.0
6
0.0
0
0.0
0
0.0
0
Y
x/o
(kg k
g-1)
1.4
9
0.3
4
0.0
0
0.0
0
0.0
0
0.0
0
0.0
0
1.0
2
0.4
2
0.0
0
0.0
0
0.0
0
0.0
0
0.0
0
0.9
1
0.6
1
0.3
4
0.0
0
0.0
0
0.0
0
0.0
0
1.2
5
0.1
3
0.0
0
0.0
0
0.0
0
q
P*10
-6
(U k
g-1 h
-1)
19.6
4
7.9
0
6.4
3
5.2
4
2.5
0
1.6
9
1.1
3
11.8
4
5.2
2
3.3
9
2.6
1
0.1
4
-1.0
3
-2.2
4
12.5
6
4.0
8
2.5
0
1.7
2
0.3
8
0.1
7
0.1
9
12.6
3
5.1
4
4.1
4
3.2
7
-0.3
2
qs
(kg k
g-1 h
-1)
0.6
7
0.4
4
0.1
6
0.1
2
0.1
6
0.9
0
0.8
8
1.3
5
0.5
6
0.3
6
0.2
8
0.1
4
0.1
2
0.1
4
1.8
4
0.6
4
0.4
4
0.3
6
0.1
6
0.1
1
0.0
7
1.5
3
0.5
5
0.5
7
1.0
0
1.2
1
q0
(kg k
g-1 h
-1)
0.3
2
0.2
0
0.1
9
0.1
6
0.1
6
0.1
6
0.1
6
0.4
3
0.3
1
0.2
2
0.2
1
0.1
8
0.1
3
0.1
3
0.6
8
0.2
0
0.1
5
0.1
3
0.1
3
0.1
3
0.1
3
0.5
2
0.2
4
0.1
5
0.1
5
0.1
5
r o
(kg O
2
m-3 h
-1)
0.1
0
0.1
3
0.1
2
0.1
0
0.1
0
0.1
0
0.1
0
0.1
2
0.1
7
0.1
5
0.1
4
0.1
2
0.0
9
0.0
9
0.1
3
0.0
9
0.0
8
0.0
7
0.0
7
0.0
7
0.0
7
0.1
2
0.1
4
0.1
0
0.1
0
0.1
0
µ
(h-1)
0.4
8
0.0
7
0.0
0
0.0
0
0.0
0
0.0
0
0.0
0
0.4
4
0.1
3
0.0
0
0.0
0
0.0
0
0.0
0
0.0
0
0.6
2
0.1
2
0.0
5
0.0
0
0.0
0
0.0
0
0.0
0
0.6
5
0.0
3
0.0
0
0.0
0
0.0
0
Cx
(kg m
-3)
0.3
1
0.6
4
0.6
4
0.6
4
0.6
4
0.6
4
0.6
4
0.2
8
0.5
4
0.6
7
0.6
7
0.6
7
0.6
7
0.6
7
0.1
9
0.4
6
0.5
5
0.5
5
0.5
5
0.5
5
0.5
5
0.2
3
0.5
8
0.6
6
0.6
6
0.6
6
t (h)
2
5
8
11
20
24
28
2
5
8
11
20
24
28
2
5
8
11
20
24
28
2
5
8
11
20
Tab
le 4
.7.b
The
variat
ions
in t
he
spec
ific
rat
es a
nd y
ield
coef
fici
ents
with c
ultiv
atio
n t
ime
at M
OT
1.
MO
T2.
HO
T1 a
nd H
OT
2 c
onditio
ns.
Conditio
n
MO
T1
MO
T2
HO
T1
HO
T2
74
4.4 Metabolic Flux Analysis
Effects of the oxygen transfer conditions on the intracellular reaction rate
distributions were investigated at limited, low, medium and high oxygen transfer
conditions by the metabolic flux analysis based on a detailed description of the
stoichiometry of all relevant biorections involved in growth and product
formation that include the glycolysis pathway, the gluconeogenesis pathway, the
anaplerotic and the pentose phosphate pathway reactions; metabolic
intermediates of the TCA cycle; the serine, alanine, aspartic acid, glutamic acid
and aromatic family amino acids, and histidine biosynthesis pathways; and the
biomass synthesis including DNA, lipids, cell components synthesis. The
stoichiometric reactions of the network used in this study are given in Appendix
G. The overall pathway was simplified by lumping some reactions into single
ones without losing representation accuracy. The extensive analysis of the broth
did not reveal any pools of metabolic by-products except SAP that was included
in the model. The exact amino acid combination of β-lactamase (Ledent et al.,
1997) and SAP (Jacobs, 1995) by B.licheniformis was used while formulating
their chemical composition. Also, the following major assumptions are
incorporated in the model:
1. All cells are assumed to show an identical behavior throughout the
bioprocess;
2. Amino acid and organic acid excretions and transportation processes
are assumed to function via passive transport mechanism;
3. Transportation of CO2, NH3 in the form NH4+, and phosphate from
the cell to the broth and from the broth to the cell are also assumed
to employ passive transport;
4. The enzyme secretion is assumed to function via passive transport
mechanism;
5. Conversion of NADPH to NADH via the transhydrogenation reaction
is reversible and not energy dependent.
75
The calculated accumulation rates of the metabolites, i.e., the organic
acids, the amino acids, β-lactamase, SAP, and the cell were used in the model to
find the intracellular flux distributions by using Equation 2.20 given in Chapter 2.
LimOT, LOT1, MOT1 and HOT2 conditions were chosen among limited, low,
medium and high oxygen transfer conditions in order to determine the effects of
oxygen on intracellular reaction rates. Considering biomass and β-lactamase
concentration profiles, the bioprocess can be divided into 4 periods as depicted
in Figure 4.16.
0
0.1
0.2
0.3
0.4
0.5
0 5 10 15 20 25t,h
CB,
kg m
-3
0
0.1
0.2
0.3
0.4
0.5
0.6
0.7
0.8
Cx,
kg m
-3
Figure 4.16 The variations of cell and beta-lactamase concentrations with the
cultivation time. LimOT: (●); LOT1:(▲); MOT1: (○); HOT2: (x).
Period I (0<t<6 h) is the exponential growth phase where the β-lactamase
synthesis starts to increase, Period II (6<t<11 h) is the stationary phase where
the β-lactamase synthesis was the highest in general, Period III (11<t<20) is
the stationary phase for β-lactamase synthesis and Period IV (20<t<30 h) is the
degradation period at HOT2 condition, whereas at MOT1 and LOT1 again β-
lactamase synthesis increased. The data of cultivation times of t1=4 h, t2=8 h,
t3=15 h, and t4=22 h were used to obtain the intracellular metabolic flux
distributions in Period I, II, III and IV respectively. The data obtained throughout
β-lactamase fermentation were exploited, using a linear approach, to calculate
Period IV
Period III
Period II
Period I
76
the specific growth rate and the uptake and the excretion rates of the
metabolites, i.e., the organic acids and the amino acids, and the secretion rates
of β-lactamase and SAP. The measured net output-rates of metabolites that are
derived from the data points of the batch-bioreactor experiments were used in
the model in order to calculate the intracellular flux distributions. The variations
in SAP concentration the with cultivation time at LimOT, LOT1, MOT1 and HOT2
conditions are given in Figure 4.17. At all the conditions, produced SAP was at
low levels. At LOT1 condition SAP was not observed in the fermentation broth.
However, at LimOT and MOT1 condition the concentration of SAP decreased with
the cultivation time whereas the concentration of SAP in the HOT2 condition
stayed constant throughout the fermentation.
0
0.01
0.02
0.03
0.04
0.05
0 5 10 15 20 25t,h
CSAP
, kg m
-3
Figure 4.17 The variations of SAP concentration with the cultivation time.
LimOT: (●); LOT1:(▲); MOT1: (○); HOT2: (x).
4.4.1 Metabolic Flux Analysis for LimOT Condition
Metabolic flux distributions for the two periods of LimOT condition are given
in Table 4.8. As seen in Table 4.8, the flux through β-lactamase synthesis (R149)
and cell formation flux (R145) decreased and reached zero from period I to
period III.
77
In period I the glycolysis pathway reactions were active; while the
gluconeogenesis pathway reactions were inactive, as expected. However, in
Period III, the reactions Pyr formation from PEP (R14) and AcCoA formation
from Pyr(R16) were inactive in the glycolysis pathway. In this period, Pyr was
produced mainly from the anapleoric reaction (R36) and from the Lac (R32).
Similar to period I, in period III the gluconeogenesis pathway reactions were
inactive.
In Period I at LimOT condition, the key intermediate R5P, synthesized for
the nucleotides and biomass components, formation was achieved by branching
at F6P through the interconversion reaction since the fluxes from G6P to both Glc
(R2) and Gluc6P (R17) were inactive and ca. 12% of the glucose was directed to
the formation of R5P from Xyl5P (R22). Nevertheless, in period III, R5P was
produced using oxidative reactions (R20) and ca. 14% of the glucose was
directed to the R5P formation by oxidative way.
In period I, Cit (R37), ICit (R38) and αKG (R39) formation reactions were
inactive in the TCA cycle, while in period III the successful operation of TCA cycle
was observed and glyoxylate shunt was inactive in both periods. As αKG is a
branch point in the TCA cycle, the magnitude of the fluxes through the αKG
formation reaction or the fluxes diverted from αKG influences the TCA cycle
fluxes and consequently, the energy generation. Among the amino acid
pathways the flux directed to glutamate from αKG (R73) is certainly important;
in period I ca. 6% of the glucose was directed to the TCA cycle via αKG.
Glucose as the carbon source, ATP is generated in the glycolysis pathway
by the substrate -level phosphorylation reactions (R10, R14), and in the TCA
cycle by both substrate-level phosphorylation (R41) and oxidative
phosphorylation (R122, R123) reactions. The total ATP generation rates were
calculated from R10, R14, R33, R41, R101, R112, R122 and R123 and they were
tabulated in Table 4.9. At LimOT condition, ATP generation rate slightly
decreased with the cultivation time from period I to period III. Throughout the
fermentation 24-53% and 40-76% of the ATP was produced by the substrate-
level phosphorylation reactions (R10, R14, and R41) and by the oxidative
phosphorylation reactions (R122, R123), respectively. In period III, according to
the model ATP was not used as the maintenance energy, however in period I ca.
16% of the total ATP produced was used for maintenance (R147).
78
In period I the formation reactions of Lac (R31) and Ac (R33) were active
while in period III they were inactive. Further, in Period III R32 catalysed by the
enzyme lactate dehydrogenase was active as Lac was converted to Pyr. Indeed
synthesis of the amino acids that are required for the biomass synthesis and
building blocks of β-lactamase is important. For glutamic acid-family amino acids
αKG, for aspartic acid-family amino acids OA, for alanine-family amino acids Pyr,
for serine-family amino acids PG3, for aromatic-family amino acids PEP and E4P,
and for histidine synthesis R5P are the branch points. Among the amino acid
pathways the flux directed to glutamate is certainly important as mentioned
above and according to the model, Glu is used for the biosynthesis of Ser (R48),
Ala (R51), Val (R53), Leu (R54), Asp (R57), mDAP (R62, Ile (R66), Phe (R69),
Tyr (R70), Gln (R74), Pro (R75) and ornithine (Orn; R76), while it is also
produced from αKG (R73) via the catabolism reactions of Ala (R79), Pro (R90),
Arg (R80), Val (R95) and His (R86) and by the biosynthesis reactions of Asn
(R58), GMP (R98), CaP (R136), UDPNAG (R137). In period I, at the branch point
of αKG in the TCA cycle, the flux through R40 was higher than the flux through
R39 due to the additional αKG synthesis through the amino acid formation
reactions of Ser (R48), Val (R53), Leu (R54) and Phe (R69). However, in period
III the flux from the TCA cycle via αKG was diverted to Glu since the flux through
R39 to R40 slightly decreased. The flux towards Asp from OA increased with the
cultivation time and all the fluxes in the aspartic acid family amino acids were
active in period I. However, in period III the formation reaction of AspSa (R59)
through formation reaction of Met (R67) were inactive. The flux through the
aromatic-family amino acids (R68), was higher in period III than in period I.
4.4.2 Metabolic Flux Analysis for LOT1 Condition
Metabolic flux distributions for four periods of LOT1 condition are given in
Table 4.8. As seen in Table 4.8, the specific cell growth rate (R145) was the
highest at period I and zero in period II, III and IV. However flux through β-
lactamase synthesis (R149) was zero in period I and the highest at period II.
In period I the glycolysis pathway reactions were active; however in Period
III the Pyr formation reaction (R14) and similar to period III at LimOT condition,
in Period II and IV at LOT1 condition both R14 and the AcCoA formation reaction
from Pyr (R16) were inactive in the glycolysis pathway. However for all period
gluconeogenesis pathway reactions were inactive.
79
In Period IV, the key intermediate R5P formation was achieved by
branching at F6P through the interconversion reaction since the fluxes from G6P
to both Glc (R2) and Gluc6P (R17) were inactive and ca. 10% of the glucose was
directed to R5P through R22. Nevertheless, in period I, II, and III R5P was
produced using oxidative reaction and in period I ca. 9% of the glucose, in
period II ca. 61% of the glucose, and in period III ca. 28% of the glucose was
directed to the R5P formation reaction.
The analysis of the TCA-cycle fluxes showed that, in period I, only the
formation of Mal (R44) and OA (R45) reactions were active in the TCA cycle.
However in period II only formation of SucCoA (R40) and Suc (R41) were
inactive in the TCA cycle. In period III the successful operation of TCA cycle was
observed while in period IV αKG (R39) and Suc (R41) formation reactions were
inactive in the TCA cycle. In the process at LOT1 condition, glyoxylate shunt was
inactive in period I and period III, but in period II and IV it was active. Moreover
in period II the reaction through Pyr synthesis from Mal (R35) was active, while
in other periods anapleoric reactions (R35, R36) were inactive.
The total ATP generation rate decreased with the cultivation time at LOT1
condition (Table 4.9). Throughout the fermentation 15-50% and 40-85% of the
ATP was produced by the substrate-level phosphorylation reactions (R10, R14,
and R41) and by the oxidative phosphorylation reactions (R122, R123),
respectively. Furthermore the ATP consumption for maintenance (R147)
increased from period I to II then decreased throughout the process at LOT1
condition.
In period III and in period IV, at the branch point of αKG in the TCA cycle,
the flux through R40 was slightly higher than the flux through R39 due to the
additional αKG synthesis through the amino acid formation reactions. However in
period II the flux from the TCA cycle via αKG was diverted to Glu since the flux
through R39 to R40 decreased.
For the synthesis of Asp and further aspartic acid-group amino acids, the
flux of the reaction that branched at OA towards Asp (R57) decreased from
period I to period II then increased with cultivation time. In Period I and II the
flux from AspSa through HSer (R64), Thr (R65), Ile (R66) and Met (R67) were
active, while in period III and period IV these reactions were inactive. The fluxes
through the aromatic-family amino acids (R68) were active in all periods.
80
Further, for the synthesis reaction of Ser from PG3 and Glu (R48) were active in
all periods except period IV.
4.4.3 Metabolic Flux Analysis for MOT1 Condition
Metabolic flux distributions for the four periods of MOT1 condition are given
in Table 4.8. As seen in Table 4.8, the specific cell growth rate (R145) was the
highest at period I and it was zero in period II, III and IV. However flux through
β-lactamase synthesis (R149) increased from period I to II and then decreased
from period II to period III and then increased from period III to IV.
In period III, the glycolysis pathway reactions were active; however, in
Period II, AcCoA formation reaction (R16) from Pyr, in period I, the Pyr
formation reaction (R14) and in period IV, similar to period II and IV at LOT1
condition, both R14 and R16 were inactive in the glycolysis pathway. Similar to
LOT1 condition, at MOT1 condition gluconeogenesis pathway reactions were
inactive in all period. Similar to period II at LOT1 condition, the reaction through
Pyr synthesis from Mal (R35) was active in period II at MOT1 condition, while in
period I, III and IV anapleoric reactions (R35, R36) were inactive.
In Period II and IV, the key intermediate R5P formation was achieved by
interconversion reaction since the fluxes from G6P to both Glc (R2) and Gluc6P
(R17) were inactive and in period II ca. 12% of glucose, in period IV ca. 20% of
glucose was directed to R5P formation through R22. Nevertheless, in period I
and III, R5P was produced by oxidative (R20) reaction and in period I ca. 25% of
the glucose and in period III ca. 16% of the glucose was directed to R5P
formation reaction.
In period I R40, and R41; in period II R39, R41, R42, and R45; and in
period III R40-R45 were inactive in the TCA cycle. However in period IV, the
successful operation of TCA cycle was observed. Moreover, the glyoxylate shunt
was inactive in period III while it was active in period I, II and IV.
The total ATP generation rate increased with the cultivation time at MOT1
condition (Table 4.9). Throughout the fermentation 33-53% and 34-58% of the
ATP was produced by the substrate-level phosphorylation reactions (R10, R14,
and R41) and by the oxidative phosphorylation reactions (R122, R123),
respectively. In period II, III and IV, according to the model ATP was not used
81
as the maintenance energy, however in period I 58% of the total ATP produced
was used for maintenance (R147).
In period II, at the branch point of αKG in the TCA cycle, the flux through
R40 was higher than the flux through R39 due to the additional αKG synthesis
through the amino acid formation reactions. However, in period I, III and IV the
flux from the TCA cycle via αKG was diverted to Glu since the flux through R39 to
R40 slightly decreased.
For the synthesis of Asp and further aspartic acid-group amino acids, the
flux of the reaction that branched at OA towards Asp (R57) increased from
period I to period II then decreased from period II to period III and then again
increased from period III to IV. In period I, II and IV the flux from AspSa
through Lys(R63), HSer (R64), Thr (R65), Ile (R66) and Met (R67) were active,
while in period III these reactions were inactive. The fluxes through the
aromatic-family amino acids (R68) and the synthesis reaction of Ser from PG3
and Glu (R48) were active in all periods.
4.4.4 Metabolic Flux Analysis for HOT2 Condition
Metabolic flux distributions for the two periods of HOT2 condition are given
in Table 4.8. As seen in Table 4.8, the specific cell growth rate (R145) and the
flux through β-lactamase synthesis decreased with cultivation time.
In period I Pyr formation reaction (R14) in the glycolysis pathway, in period
III, similar to period IV at MOT1 condition, in addition to R14, the AcCoA
formation reaction (R16) from Pyr were inactive. Similar to LOT1 and MOT1
condition, in period I and in period III the gluconeogenesis pathway reactions
were inactive.
In period III at HOT2 condition, the key intermediate R5P formation was
achieved by branching at F6P through the interconversion reaction and ca. 20%
of the glucose was diverted to formation of R5P through R22. Nevertheless, in
period I, R5P was produced using oxidative (R20) reaction and ca. 45% of the
glucose was directed to R5P formation reaction.
82
In period I the reactions R37, R38, and R39; and in period III R40, and
R41 were inactive in the TCA cycle. In the process, the glyoxylate shunt was
inactive in period I while it is active in period III.
The total ATP generation rate slightly increased with the cultivation time at
HOT2 condition (Table 4.9). Throughout the fermentation 20-49% and 51-80%
of the ATP was produced by the substrate-level phosphorylation reactions (R10,
R14, and R41) and by the oxidative phosphorylation reactions (R122, R123),
respectively. According to the model ATP was not used as the maintenance
energy, in period III while in period I 37% of the total ATP produced was used
for maintenance (R147).
In period I, at the branch point of αKG in the TCA cycle, the flux through
R40 was higher than the flux through R39 due to the additional αKG synthesis
through the amino acid formation reactions of Ser (R48), Ala (R51), Val(R53),
Leu (R54), Phe (R69), Tyr (R70). However in period III, the flux from the TCA
cycle via αKG was diverted to Glu since the flux through R39 to R40 decreased.
The flux towards Asp from OA increased with the cultivation time and all the
fluxes through the aspartic acid family amino acids were active throughout the
bioprocess. Moreover, the flux through the aromatic-family amino acids (R68)
and serine-family amino acids (R48) were higher in period III than in period I.
Metabolic flux analysis results show that with glucose as the carbon source,
energy is generated first in the glycolysis pathway by the substrate level
phosphorylation and then in the TCA cycle by the oxidative phosphorylation
reactions. Although it is expected that ATP generation would be the highest at
high oxygen transfer condition, the comparison of the ATP generation at LimOT,
LOT1, MOT1, and HOT2 showed a different profile that verifies the regulatory
responses of cell in the metabolic reaction network.
83
t=15
9.9
330
0.0
000
0.0
000
9.9
330
0.0
000
0.0
000
0.0
000
7.9
490
0.0
000
15.8
950
0.0
000
13.9
050
0.0
000
0.0
000
HO
T2 c
onditio
n f
luxe
s
mm
ol g
-1 D
W h
-1
t=4
3.4
600
0.0
000
0.0
000
1.8
850
0.0
000
0.0
000
0.0
000
1.8
480
0.0
000
3.6
580
0.0
000
3.5
190
0.0
000
0.0
000
t=22
10.7
640
0.0
000
0.0
000
10.7
64
0.0
000
0.0
000
0.0
000
8.6
340
0.0
000
17.2
380
0.0
000
15.0
580
0.0
000
0.0
000
t=15
6.5
500
0.0
000
0.0
000
5.5
030
0.0
000
0.0
000
0.0
000
5..
1770
0.0
000
10.7
040
0.0
000
9.6
900
0.0
000
1.0
930
t=8
3.8
190
0.0
000
0.0
000
3.8
19
0.0
000
0.0
000
0.0
000
3.3
430
0.0
000
6.3
200
0.0
000
6.2
050
0.0
000
1.4
330
MO
T1 c
onditio
n f
luxe
s
mm
ol g
-1 D
W h
-1
t=4
3.0
900
0.0
000
0.0
000
2.2
900
0.0
000
0.0
000
0.0
000
2.2
740
0.0
000
4.7
040
0.0
000
4.0
420
0.0
000
0.0
000
t=22
0.9
260
0.0
000
0.0
000
0.9
260
0.0
000
0.0
000
0.0
000
0.8
330
0.0
000
1.4
810
0.0
000
1.4
810
0.0
000
0.0
000
t=15
0.4
630
0.0
000
0.0
000
0.3
340
0.0
000
0.0
000
0.0
000
0.3
340
0.0
000
0.7
100
0.0
000
0.6
360
0.0
000
0.0
000
t=8
2.0
370
0.0
000
0.0
000
0.7
890
0.0
000
0.0
000
0.0
000
1.3
120
0.0
000
3.0
270
0.0
000
2.6
770
0.0
000
0.0
000
LOT
1 c
onditio
n f
luxe
s
mm
ol g
-1 D
W h
-1
t=4
6.5
500
0.0
000
0.0
000
5.9
250
0.0
000
0.0
000
0.0
000
5.9
100
0.0
000
11.8
670
0.0
000
11.7
990
0.0
000
4.7
860
t=15
2.7
270
0.0
000
0.0
000
2.3
380
0.0
000
0.0
000
0.0
000
2.3
380
0.0
000
4.2
860
0.0
000
4.2
860
0.0
000
0.0
000
Lim
OT c
onditio
n f
luxe
s
mm
ol g
-1 D
W h
-1
t=4
6.2
500
0.0
000
0.0
000
6.2
060
0.0
000
0.0
000
0.0
000
5.4
300
0.0
000
10.7
470
0.0
000
9.8
190
0.0
000
2.3
110
Tab
le 4
.8 M
etab
olic
flu
x dis
trib
ution o
f β-
lact
amas
e fe
rmen
tation
of
B.lic
hen
iform
is a
t Li
mO
T,
LOT
1,
MO
T1,
and H
OT
2 c
onditio
ns
R#
1
2
3
4
5
6
7
8
9
10
11
12
13
14
84
t=15
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
1.9
840
0.0
007
0.0
000
0.0
007
0.0
000
0.0
000
1.9
850
HO
T2 c
onditio
n f
luxe
s
mm
ol g
-1 D
W h
-1
t=4
0.0
000
0.1
130
1.5
620
0.0
000
0.0
000
1.5
620
0.0
000
0.0
290
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
290
t=22
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
2.1
300
0.0
090
0.0
000
0.0
090
0.0
000
0.0
000
2.1
380
t=15
0.0
000
2.7
660
1.0
470
0.0
000
0.0
000
1.0
470
0.0
000
0.3
260
0.3
490
0.0
000
0.3
490
0.0
000
0.0
000
0.6
750
t=8
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.4
760
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.4
760
MO
T1 c
onditio
n f
luxe
s
mm
ol g
-1 D
W h
-1
t=4
0.0
000
3.2
620
0.7
710
0.0
000
0.0
000
0.7
710
0.0
000
0.0
000
0.2
380
0.0
000
0.2
380
0.0
000
0.0
000
0.2
380
t=22
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
930
0.0
930
0.0
000
0.0
930
0.0
000
0.0
000
0.1
850
t=15
0.0
000
0.0
940
0.1
290
0.0
000
0.0
000
0.1
290
0.0
000
0.0
000
0.0
430
0.0
000
0.0
430
0.0
000
0.0
000
0.0
430
t=8
0.0
000
0.0
000
1.2
480
0.0
000
0.0
000
1.2
480
0.5
230
0.0
000
0.4
220
0.0
000
0.4
220
0.0
000
0.1
020
0.0
000
LOT
1 c
onditio
n f
luxe
s
mm
ol g
-1 D
W h
-1
t=4
0.0
000
3.3
930
0.5
980
0.0
000
0.0
000
0.5
980
0.0
000
0.0
000
0.1
160
0.0
000
0.1
160
0.0
000
0.0
000
0.1
160
t=15
0.0
000
0.0
000
0.3
900
0.0
000
0.0
000
0.3
900
0.0
000
0.0
000
0.3
900
0.0
000
0.3
900
0.0
000
0.0
000
0.3
900
Lim
OT c
onditio
n f
luxe
s
mm
ol g
-1 D
W h
-1
t=4
0.0
000
2.3
070
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.7
510
0.0
000
0.0
610
0.0
000
0.0
610
0.0
000
0.6
900
Tab
le 4
.8 C
ontinued
R#
15
16
17
18
19
20
21
22
23
24
25
26
27
28
85
t=15
0.0
007
0.0
000
0.0
860
0.0
000
0.0
000
8.8
440
0.0
000
0.0
000
5.9
690
5.9
690
0.0
070
0.0
000
0.0
000
0.0
000
HO
T2 c
onditio
n f
luxe
s
mm
ol g
-1 D
W h
-1
t=4
0.0
000
0.0
020
0.0
000
0.4
190
0.0
000
0.3
360
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
1.3
330
2.1
020
0.0
000
t=22
0.0
090
0.0
000
0.0
000
0.0
780
0.0
000
12.0
670
0.0
000
0.0
000
7.8
870
7.8
870
1.8
010
1.6
710
1.6
710
0.0
000
t=15
0.3
490
0.0
000
6.6
870
0.0
000
3.6
010
0.0
000
0.0
000
0.0
000
0.0
090
0.0
090
0.0
090
0.0
000
0.0
000
0.0
000
t=8
0.0
000
0.0
000
0.0
005
0.0
000
0.0
000
4.2
320
5.8
090
0.0
000
2.3
510
2.3
480
0.0
000
0.3
460
0.0
000
0.0
000
MO
T1 c
onditio
n f
luxe
s
mm
ol g
-1 D
W h
-1
t=4
0.2
340
0.0
000
0.0
070
0.0
000
1.4
150
0.0
000
0.0
000
0.0
000
0.8
500
0.8
500
0.1
980
0.0
000
0.0
000
0.0
000
t=22
0.0
930
0.0
000
0.0
000
0.0
000
0.0
000
0.9
170
0.0
000
0.0
000
0.5
850
0.5
850
0.0
000
0.0
030
0.0
000
0.2
750
t=15
0.0
430
0.0
000
0.0
000
0.5
140
0.0
000
1.8
110
0.0
000
0.0
000
2.0
150
2.0
150
2.0
150
2.0
310
2.0
310
0.0
000
t=8
0.4
220
0.0
000
0.0
000
0.0
000
0.0
000
0.0
930
0.5
620
0.0
000
0.9
420
0.9
420
0.1
030
0.0
000
0.0
000
0.0
000
LOT
1 c
onditio
n f
luxe
s
mm
ol g
-1 D
W h
-1
t=4
0.1
120
0.0
000
6.6
870
0.0
000
3.4
140
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
t=15
0.3
900
0.0
000
0.0
000
0.0
630
0.0
000
3.4
850
0.0
000
0.8
110
1.7
130
1.7
130
1.7
130
1.7
110
0.9
320
0.0
000
Lim
OT c
onditio
n f
luxe
s
mm
ol g
-1 D
W h
-1
t=4
0.0
000
0.0
680
6.6
480
0.0
000
1.9
950
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.3
480
0.3
480
0.0
000
Tab
le 4
.8 C
ontinued
R#
29
30
31
32
33
34
35
36
37
38
39
40
41
42
86
t=15
5.9
620
5.9
640
11.9
270
5.9
620
5.9
620
1.9
910
0.0
030
0.0
008
0.0
000
1.0
990
0.0
040
1.0
950
1.9
840
0.0
005
HO
T2 c
onditio
n f
luxe
s
mm
ol g
-1 D
W h
-1
t=4
2.1
020
3.7
110
3.7
110
0.0
000
0.0
000
0.1
390
0.0
580
0.0
270
0.0
630
0.9
200
0.8
310
0.0
880
1.5
890
1.5
340
t=22
7.7
570
7.8
190
13.9
050
6.0
860
6.0
860
2.1
800
0.0
230
0.0
000
0.0
000
0.1
480
0.0
520
0.0
960
2.1
210
0.0
140
t=15
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
1.0
140
0.0
000
0.0
000
0.0
000
0.0
190
0.0
000
0.0
190
1.0
240
0.0
000
t=8
2.7
210
3.4
610
0.0
000
2.3
480
2.3
480
0.1
150
0.0
030
0.0
000
0.0
000
0.0
380
0.0
300
0.0
070
0.4
760
0.3
670
MO
T1 c
onditio
n f
luxe
s
mm
ol g
-1 D
W h
-1
t=4
0.6
530
0.7
980
1.4
500
0.6
530
0.6
530
0.6
620
0.1
250
0.0
540
0.0
000
0.1
480
0.0
710
0.0
770
0.5
290
0.0
000
t=22
0.5
880
0.8
970
1.4
820
0.5
850
0.5
850
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
t=15
2.0
220
2.0
230
2.0
230
0.0
000
0.0
000
0.0
750
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
860
0.0
000
t=8
0.8
390
0.8
830
1.1
610
0.8
390
0.8
390
0.3
500
0.0
240
0.0
060
0.0
000
1.5
560
0.0
210
1.5
350
0.3
030
0.0
010
LOT
1 c
onditio
n f
luxe
s
mm
ol g
-1 D
W h
-1
t=4
0.0
000
0.2
830
0.2
830
0.0
000
0.0
000
0.0
670
0.0
000
0.0
370
0.0
860
0.1
500
0.0
640
0.0
860
0.4
790
0.1
890
t=15
1.74
50
6.87
60
6.87
60
0.00
00
0.00
00
0.00
00
0.00
00
0.00
00
0.00
00
1.80
00
0.00
00
1.80
00
0.00
00
0.00
00
Lim
OT c
onditio
n f
luxe
s
mm
ol g
-1 D
W h
-1
t=4
0.3
480
0.4
520
0.4
520
0.0
000
0.0
000
0.9
290
0.1
540
0.0
620
0.0
000
0.1
990
0.1
120
0.0
870
0.8
060
0.0
240
Tab
le 4
.8 C
ontinued
R#
43
44
45
46
47
48
49
50
51
52
53
54
55
56
87
t=15
8.7
940
0.0
050
8.7
800
8.7
730
8.7
730
8.7
730
8.7
730
0.0
070
0.0
060
0.0
020
0.0
008
1.9
860
0.0
009
0.0
020
HO
T2 c
onditio
n f
luxe
s
mm
ol g
-1 D
W h
-1
t=4
3.7
110
0.0
370
1.9
520
1.8
330
1.8
330
1.8
330
1.8
330
0.1
190
0.1
000
0.0
500
0.0
190
0.0
280
0.0
050
0.0
230
t=22
10.4
780
0.0
460
10.3
500
10.1
600
10.1
600
10.1
600
10.1
600
0.1
900
0.1
810
0.0
500
0.0
090
2.1
470
0.0
210
0.0
240
t=15
0.0
190
7.6
120
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
1.0
240
0.0
000
0.0
000
t=8
4.6
170
0.0
020
4.2
400
4.2
290
4.2
290
4.2
290
4.2
290
0.0
110
0.0
100
0.0
040
0.0
010
0.4
760
0.0
000
0.3
670
MO
T1 c
onditio
n f
luxe
s
mm
ol g
-1 D
W h
-1
t=4
0.6
000
0.0
000
0.3
570
0.2
320
0.2
320
0.2
320
0.2
320
0.1
250
0.0
940
0.0
490
0.0
310
0.4
720
0.0
360
0.0
230
t=22
0.9
580
0.0
250
0.8
870
0.8
870
0.8
870
0.8
870
0.8
870
0.0
000
0.0
000
0.0
000
0.0
000
0.2
780
0.0
000
0.2
780
t=15
0.5
430
0.0
000
0.5
450
0.5
450
0.5
450
0.5
450
0.5
450
0.0
000
0.0
000
0.0
000
0.0
000
0.0
860
0.0
000
0.0
000
t=8
0.2
190
0.0
180
0.1
160
0.0
340
0.0
340
0.0
340
0.0
340
0.0
810
0.0
760
0.0
200
0.0
060
0.3
200
0.0
100
0.0
090
LOT
1 c
onditio
n f
luxe
s
mm
ol g
-1 D
W h
-1
t=4
1.2
610
0.0
450
0.8
200
0.0
510
0.0
510
0.0
510
0.0
510
0.7
690
0.7
470
0.0
430
0.0
220
0.2
270
0.0
270
0.0
210
t=15
4.35
30
0.00
20
0.00
00
0.00
00
0.00
00
0.00
00
0.00
00
0.00
00
0.00
00
0.00
00
0.00
00
0.77
90
0.00
00
0.77
90
Lim
OT c
onditio
n f
luxe
s
mm
ol g
-1 D
W h
-1
t=4
0.6
750
0.0
990
0.2
460
0.0
950
0.0
950
0.0
950
0.0
950
0.1
500
0.1
120
0.0
770
0.0
380
0.6
220
0.0
180
0.0
000
Tab
le 4
.8 C
ontinued
R#
57
58
59
60
61
62
63
64
65
66
67
68
69
70
88
t=15
1.9
830
1.9
830
17.5
890
0.0
090
0.0
020
0.0
020
0.0
020
0.0
020
1.9
790
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
HO
T2 c
onditio
n f
luxe
s
mm
ol g
-1 D
W h
-1
t=4
0.0
000
0.0
000
6.2
310
1.7
510
0.0
380
0.0
560
0.0
510
0.0
510
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
t=22
2.1
070
2.1
070
21.2
440
0.1
380
0.0
000
0.0
490
0.0
490
0.0
490
2.0
040
0.0
000
0.0
000
0.0
000
0.0
040
0.0
000
t=15
1.0
240
1.0
240
0.2
080
7.6
200
0.0
000
0.0
000
0.0
000
0.0
000
0.8
520
0.0
000
7.6
020
0.0
000
0.0
000
0.0
000
t=8
0.1
090
0.1
090
8.8
790
0.3
720
0.0
190
0.0
000
0.0
000
0.0
000
0.1
030
0.0
080
0.0
000
0.0
000
0.0
010
0.0
000
MO
T1 c
onditio
n f
luxe
s
mm
ol g
-1 D
W h
-1
t=4
0.4
130
0.4
130
1.7
380
0.3
480
0.0
360
0.1
030
0.0
930
0.0
930
0.3
120
0.0
000
0.0
090
0.0
000
0.0
000
0.0
000
t=22
0.0
000
0.0
000
1.8
360
0.0
530
0.0
000
0.0
310
0.0
310
0.0
310
0.0
060
0.0
310
0.0
000
0.0
000
0.0
000
0.0
000
t=15
0.0
860
0.0
860
1.0
190
0.0
000
0.0
000
0.0
010
0.0
010
0.0
010
0.1
110
0.0
160
0.0
000
0.0
000
0.0
000
0.0
000
t=8
0.3
020
0.3
020
0.5
890
0.0
770
0.0
160
0.0
420
0.0
420
0.0
420
0.2
600
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
LOT
1 c
onditio
n f
luxe
s
mm
ol g
-1 D
W h
-1
t=4
0.1
790
0.1
790
1.9
500
0.5
260
0.0
320
0.0
540
0.0
450
0.0
450
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
t=15
0.00
00
0.00
00
4.35
50
4.35
50
0.00
00
4.35
20
4.35
20
4.35
20
0.00
00
4.35
20
0.00
00
0.00
00
0.00
00
0.00
00
Lim
OT c
onditio
n f
luxe
s
mm
ol g
-1 D
W h
-1
t=4
0.6
040
0.6
040
0.5
740
0.5
150
0.0
580
0.0
150
0.0
000
0.0
000
0.5
440
0.5
660
0.0
000
0.0
000
0.0
000
0.0
000
Tab
le 4
.8 C
ontinued
R#
71
72
73
74
75
76
77
78
79
80
81
82
83
84
89
t=15
0.0
000
0.0
000
0.0
000
1.1
020
0.0
000
0.0
000
0.0
000
0.0
000
1.9
840
0.0
000
0.0
000
0.0
000
0.0
005
0.0
000
HO
T2 c
onditio
n f
luxe
s
mm
ol g
-1 D
W h
-1
t=4
0.0
000
1.5
190
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
180
0.0
000
0.7
690
0.0
210
1.5
550
0.0
180
t=22
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
210
0.0
000
0.0
470
2.0
970
0.0
000
0.0
000
0.0
000
0.0
140
0.0
000
t=15
0.0
220
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
100
0.8
520
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
t=8
0.0
000
0.3
660
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.1
100
0.3
730
0.0
260
0.0
000
0.3
670
0.0
000
MO
T1 c
onditio
n f
luxe
s
mm
ol g
-1 D
W h
-1
t=4
0.0
000
0.0
320
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.4
080
0.0
000
0.0
000
0.0
450
0.0
450
0.0
370
t=22
0.0
080
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
160
0.0
000
0.0
060
0.2
780
0.0
000
0.0
000
0.0
000
0.0
000
t=15
0.0
110
0.0
000
0.0
000
0.0
010
0.0
000
0.0
000
0.0
000
0.0
160
0.0
930
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
t=8
0.0
000
0.0
000
0.0
000
1.4
940
0.0
000
0.0
000
0.0
000
0.0
000
0.3
220
0.0
000
0.0
000
0.0
000
0.0
010
0.0
000
LOT
1 c
onditio
n f
luxe
s
mm
ol g
-1 D
W h
-1
t=4
0.2
250
0.1
750
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.6
760
0.0
000
0.0
000
0.0
000
0.0
420
0.2
310
0.0
350
t=15
0.00
40
0.00
00
0.00
00
1.80
00
0.00
00
0.00
00
0.00
00
0.00
00
0.00
00
0.77
90
0.00
00
0.00
00
0.00
00
0.00
00
Lim
OT c
onditio
n f
luxe
s
mm
ol g
-1 D
W h
-1
t=4
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.6
430
0.0
000
0.0
000
0.0
690
0.0
920
0.0
570
Tab
le 4
.8 C
ontinued
R#
85
86
87
88
89
90
91
92
93
94
95
96
97
98
90
t=15
0.0
000
0.0
005
0.0
000
0.0
000
0.0
000
0.0
005
1.9
930
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
HO
T2 c
onditio
n f
luxe
s
mm
ol g
-1 D
W h
-1
t=4
0.0
180
1.5
540
0.0
000
0.0
020
0.0
020
1.5
380
3.2
780
0.0
340
0.0
340
0.0
320
0.0
150
0.0
020
0.0
000
0.0
020
t=22
0.0
000
0.0
140
0.0
000
0.0
000
0.0
000
0.0
140
2.2
350
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
t=15
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
8.6
360
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
t=8
0.0
000
0.3
670
0.0
000
0.0
000
0.0
000
0.3
670
0.8
440
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
MO
T1 c
onditio
n f
luxe
s
mm
ol g
-1 D
W h
-1
t=4
0.0
370
0.0
410
0.0
000
0.0
030
0.0
030
0.0
070
0.7
520
0.0
720
0.0
720
0.0
690
0.0
320
0.0
030
0.0
000
0.0
030
t=22
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
560
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
t=15
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
880
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
t=8
0.0
000
0.0
010
0.0
000
0.0
000
0.0
000
0.0
010
0.3
770
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
LOT
1 c
onditio
n f
luxe
s
mm
ol g
-1 D
W h
-1
t=4
0.0
350
0.2
280
0.0
000
0.0
030
0.0
030
0.1
960
0.8
590
0.0
680
0.0
680
0.0
650
0.0
300
0.0
030
0.0
000
0.0
030
t=15
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
4.3
530
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
Lim
OT c
onditio
n f
luxe
s
mm
ol g
-1 D
W h
-1
t=4
0.0
570
0.0
870
0.0
000
0.0
050
0.0
050
0.0
350
1.0
980
0.1
100
0.1
100
0.1
050
0.0
490
0.0
050
0.0
000
0.0
050
Tab
le 4
.8 C
ontinued
R#
99
100
101
102
103
104
105
106
107
108
109
110
111
112
91
t=15
0.0
000
0.0
000
0.0
020
0.0
008
0.0
005
0.0
005
0.0
000
40.2
250
0.0
000
0.4
700
15.8
340
9.0
240
0.0
000
19.5
800
HO
T2 c
onditio
n f
luxe
s
mm
ol g
-1 D
W h
-1
t=4
0.0
020
0.0
020
0.0
000
0.0
190
0.0
570
1.5
760
0.0
210
8.6
590
0.0
000
8.7
980
5.3
980
6.4
940
0.0
000
7.9
070
t=22
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
220
0.0
000
0.0
000
7.8
480
0.0
000
4.8
590
0.0
000
1.2
280
t=15
0.0
030
0.0
030
0.0
000
0.0
220
0.0
990
0.2
740
0.3
490
3.8
020
0.0
000
6.7
350
0.0
000
3.6
880
0.0
000
2.2
700
t=8
0.0
000
0.0
000
0.0
010
0.0
010
0.0
003
0.3
670
0.0
000
12.2
150
0.0
000
0.0
000
6.9
970
4.3
360
0.0
000
9.3
480
MO
T1 c
onditio
n f
luxe
s
mm
ol g
-1 D
W h
-1
t=4
0.0
030
0.0
030
0.0
340
0.0
310
0.0
570
0.0
900
0.0
000
3.0
270
0.0
000
7.3
930
0.8
260
4.8
940
0.0
000
2.4
760
t=22
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
080
3.8
930
0.0
000
0.2
460
1.4
750
1.3
920
0.0
000
1.8
340
t=15
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
110
0.0
000
0.0
000
6.0
220
2.5
690
4.3
940
0.0
000
1.0
780
t=8
0.0
000
0.0
000
0.0
170
0.0
060
0.0
010
0.0
010
0.0
000
0.0
000
0.0
000
7.5
610
2.3
340
3.7
630
0.0
000
0.9
590
LOT
1 c
onditio
n f
luxe
s
mm
ol g
-1 D
W h
-1
t=4
0.0
030
0.0
030
0.0
000
0.0
220
0.0
990
0.2
740
0.3
490
3.8
020
0.0
000
6.7
350
0.0
000
3.6
880
0.0
000
2.2
700
t=15
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
040
4.4
430
0.0
000
12.8
770
3.5
460
7.9
870
0.0
000
4.3
530
Lim
OT c
onditio
n f
luxe
s
mm
ol g
-1 D
W h
-1
t=4
0.0
050
0.0
050
0.0
000
0.0
380
0.1
610
0.1
610
0.0
510
3.6
360
0.0
000
4.8
520
0.3
480
3.8
690
0.0
000
1.0
090
Tab
le 4
.8 C
ontinued
R#
113
114
115
116
117
118
119
120
121
122
123
124
125
126
92
t=15
0.0
000
0.0
020
1.9
930
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
020
0.0
000
0.0
000
0.0
000
0.0
000
HO
T2 c
onditio
n f
luxe
s
mm
ol g
-1 D
W h
-1
t=4
0.0
000
0.0
460
3.2
890
0.1
710
0.0
000
0.0
100
0.0
020
0.0
020
0.0
210
0.0
850
0.0
060
0.0
020
0.0
020
0.0
020
t=22
0.0
000
0.0
050
2.2
350
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
490
0.0
000
0.0
000
0.0
000
0.0
000
t=15
0.0
000
0.0
000
8.6
360
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
t=8
0.0
000
0.0
000
0.8
440
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
MO
T1 c
onditio
n f
luxe
s
mm
ol g
-1 D
W h
-1
t=4
0.0
000
0.0
850
0.7
740
0.3
640
0.0
000
0.0
220
0.0
040
0.0
040
0.0
440
0.1
650
0.0
120
0.0
050
0.0
040
0.0
040
t=22
0.0
000
0.0
000
0.0
560
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
310
0.0
000
0.0
000
0.0
000
0.0
000
t=15
0.0
000
0.0
000
0.0
880
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
010
0.0
000
0.0
000
0.0
000
0.0
000
t=8
0.0
000
0.0
110
0.3
770
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
420
0.0
000
0.0
000
0.0
000
0.0
000
LOT
1 c
onditio
n f
luxe
s
mm
ol g
-1 D
W h
-1
t=4
0.0
000
0.0
590
0.8
800
0.3
430
0.0
000
0.0
210
0.0
040
0.0
040
0.0
410
0.1
130
0.0
110
0.0
040
0.0
040
0.0
040
t=15
0.0
000
0.0
000
4.3
530
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
4.3
520
0.0
000
0.0
000
0.0
000
0.0
000
Lim
OT c
onditio
n f
luxe
s
mm
ol g
-1 D
W h
-1
t=4
0.0
000
0.1
000
1.1
330
0.5
570
0.0
000
0.0
340
0.0
060
0.0
060
0.0
670
0.1
100
0.0
180
0.0
070
0.0
060
0.0
060
Tab
le 4
.8 C
ontinued
R#
127
128
129
130
131
132
133
134
135
136
137
138
139
140
93
t=15
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
001
0.0
000
2.8
360
0.0
001
HO
T2 c
onditio
n f
luxe
s
mm
ol g
-1 D
W h
-1
t=4
0.0
020
0.0
140
0.0
000
0.0
010
0.0
800
0.0
000
10.6
580
0.0
000
0.0
020
t=22
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
003
0.0
000
4.4
590
0.0
030
t=15
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
270
0.0
000
t=8
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
6.9
680
0.0
003
MO
T1 c
onditio
n f
luxe
s
mm
ol g
-1 D
W h
-1
t=4
0.0
040
0.0
290
0.0
000
0.0
030
0.1
700
0.0
000
8.3
26
0.0
000
0.0
000
t=22
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
620
0.0
000
t=15
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
14.3
970
0.5
350
0.0
000
t=8
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
16.0
800
0.0
000
0.0
010
LOT
1 c
onditio
n f
luxe
s
mm
ol g
-1 D
W h
-1
t=4
0.0
040
0.0
270
0.0
000
0.0
030
0.1
600
0.0
000
15.6
840
0.9
770
0.0
000
t=15
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
0.0
000
Lim
OT c
onditio
n f
luxe
s
mm
ol g
-1 D
W h
-1
t=4
0.0
060
0.0
440
0.0
000
0.0
040
0.2
600
0.0
000
3.9
800
0.2
230
0.0
005
Tab
le 4
.8 C
ontinued
R#
141
142
143
144
145
146
147
148
149
94
Table 4.9 ATP generation throughout the fermentation. LimOT Period I Period III
mmol g-1 DW h-1 ATP ATP
R# ATP% ATP%
10 10.747 42.21 4.286 19.80 14 2.311 9.08 0.000 0.00 33 1.995 7.84 0.000 0.00 41 0.348 1.37 0.932 4.31 101 0.000 0.00 0.000 0.00 112 0.005 0.02 0.000 0.00 122 9.704 38.12 12.877 59.50 123 0.348 1.37 3.546 16.39
Total 25.458 100 21.641 100
LOT1 Period I Period II Period III Perıod IV
mmol g-1 DW h-1 ATP ATP ATP ATP R# ATP% ATP% ATP% ATP%
10 11.867 35.38 3.027 14.78 0.710 4.09 1.481 42.95
14 4.786 14.27 0.000 0.00 0.000 0.00 0.000 0.00
33 3.414 10.18 0.000 0.00 0.000 0.00 0.000 0.00
41 0.000 0.00 0.000 0.00 2.031 11.70 0.000 0.00
101 0.000 0.00 0.000 0.00 0.000 0.00 0.000 0.00
112 0.003 0.01 0.003 0.01 0.000 0.00 0.000 0.00
122 13.470 40.16 15.122 73.82 12.044 69.40 0.492 14.27
123 0.000 0.00 2.334 11.39 2.569 14.80 1.475 42.78
Total 33.540 100 20.486 100 17.354 100 3.448 100
MOT1 Period I Period II Period III Period IV
mmol g-1 DW h-1 ATP ATP ATP ATP R# ATP% ATP% ATP% ATP%
10 4.704 32.80 6.320 42.85 10.704 46.05 17.238 45.16
14 0.000 0.00 1.433 9.72 1.093 4.70 0.000 0.00
33 1.415 9.87 0.000 0.00 3.601 15.49 0.000 0.00
41 0.000 0.00 0.000 0.00 0.000 0.00 1.671 4.38
101 0.000 0.00 0.000 0.00 0.000 0.00 0.000 0.00
112 0.003 0.02 0.000 0.00 0.000 0.00 0.000 0.00
122 7.393 51.55 0.000 0.00 7.848 33.76 1.430 3.75
123 0.826 5.76 6.997 47.44 0.000 0.00 17.832 46.72
Total 14.341 100 14.750 100 23.246 100 38.171 100
HOT2 Period I Period III mmol g-1 DW h-1 ATP ATP
R# ATP% ATP% 10 3.658 12.72 15.895 48.65 14 0.000 0.00 0.000 0.00 33 0.000 0.00 0.000 0.00 41 2.102 7.31 0.000 0.00 101 0.000 0.00 0.000 0.00 112 0.002 0.01 0.000 0.00 122 17.596 61.19 0.940 2.88 123 5.398 18.77 15.834 48.47
Total 28.756 100 32.669 100
95
CHAPTER 5
CONCLUSION
This study focuses on, the effects of oxygen transfer on β-lactamase
production by Bacillus licheniformis on a defined medium. In order to clarify the
oxygen transfer effects on the production of β-lactamase, firstly a glucose based
defined medium was designed and using this medium, the effects of the
bioreactor operation parameters, i.e., pH and temperature, on β-lactamase
activity and cell formation were investigated in laboratory scale bioreactors.
Thereafter, using the optimized medium the effects of oxygen transfer on cell
generation, substrate consumption, product (β-lactamase) and by-products
formation were investigated in the pilot scale bioreactor. Finally, the influence of
oxygen transfer conditions on the intracellular reaction rates in β-lactamase
production by B.licheniformis under well-defined batch bioreactor conditions was
investigated using metabolic flux analysis to evaluate the effects of oxygen on
the metabolism. In this context the following conclusions were drawn:
1. In order to design a defined medium firstly yeast extract was
omitted from the medium found in the study of Çalık and Çelik
(2004), and medium, that contained (kg m-3): glucose, 8;
(NH4)2HPO4, 4.7 and the salt solution in which the β-lactamase
activity was obtained as 60 U cm-3 was considered as the starting
point for medium design experiments and the medium named as
reference production medium (RPM).
2. The effect of (NH4)2HPO4 concentration was investigated within the
range corresponding to initial nitrogen concentration of 0.0 – 4.0 kg
m-3 on β- lactamase activity at 37°C with an initial pH of 7.2. The
highest β-lactamase activity was obtained at CN0 = 7.1 kg m-3 as
A=76 U cm-3.
3. The effect of pH control on β-lactamase production was investigated
in the initial pH range of 5.8-8.0, in media with NaH2PO4 - Na2HPO4
buffer, and without buffer (the uncontrolled-pH operation).
96
Uncontrolled-pH operation was found to be more favorable for β-
lactamase production. Furthermore, the effects of pH and
temperature were investigated in the medium without buffer.
T=37°C, and pH=7.5 were found to be the favorable condition for β-
lactamase production.
4. The effects of glucose concentration on β-lactamase production were
investigated in the range of CG°=6.0, 7.0, 8.0, 9.0, 10.0, 11.0, and
12.0 kg m-3, in the medium containing 7.1 kg m-3 (NH4)2HPO4 and
the salt solution at a cultivation temperature of T=37°C with an
initial pH of 7.5. The activity of β-lactamase did not change
significantly in this range and CG°=7 kg m-3 was selected as an
initial glucose concentration.
5. As a result of the medium design experiments, the highest β-
lactamase activity was obtained as 115 U cm-3, in the medium
containing 7.0 kg m-3 glucose, 7.1 kg m-3 (NH4)2HPO4, and the salt
solution at pH=7.5, T= 37°C, N=200 min-1, V=33 cm3, which was 2-
fold higher than the activity obtained in the RPM.
6. Using the optimized defined medium, T and pH obtained in the
laboratory scale experiments the effects of oxygen transfer on
fermentation and oxygen transfer characteristics were investigated
in the pilot scale bioreactor system at seven oxygen transfer
conditions. Throughout the bioprocess, dissolved oxygen, pH,
glucose, cell, amino acid and organic acid concentrations, β-
lactamase activity, liquid phase mass transfer coefficient, specific
growth rate, and yield coefficients were determined.
7. Considering the CO profiles, Q0/VR = 0.2 vvm and N =250 min-1
(LimOT) is regarded as “limited-oxygen transfer” condition; Q0/VR =
0.5 vvm and N =250 min-1 (LOT1), and Q0/VR = 0.2 vvm and N
=500 min-1 (LOT2) are regarded as “low-oxygen transfer”
conditions; Q0/VR = 0.5 vvm and N =500 min-1 (MOT1), Q0/VR = 0.2
vvm and N =750 min-1 (MOT2) are regarded as “medium oxygen
transfer” conditions; and lastly Q0/VR = 1 vvm and N =500 min-1
(HOT1) and Q0/VR = 0.5 vvm and N =750 min-1 (HOT2) are regarded
as “high-oxygen transfer” condition.
97
8. At LimOT and to an extent at LOT1 conditions the CO exhibited
sudden drop at the early hours of the fermentation and at t= 1-27 h
for LimOT and, at t=2-10.5 h for LOT1 the transferred oxygen was
totally consumed. When the OTR was higher, i.e., at LOT2, MOT1,
and MOT2 conditions, a decrease and/or an increase in the dissolved
oxygen level with cultivation time was observed depending on the
metabolic stage of the growth. Further, at HOT1 and HOT2
conditions, although the biomass concentration increased, DO
concentration did not change considerably throughout the
bioprocess as the OTR was high enough.
9. The locus of pH vs time profiles were similar at LOT2, MOT1, MOT2,
HOT1, and HOT2 conditions, and pH has a tendency to decrease until
t=10 h; thereafter, it reached to the stationary phase. However, at
LOT1 and LimOT conditions the decrease rate of pH was higher than
the other conditions. At LimOT condition where the lowest pH was
observed, the pH of the fermentation broth decreased until t= 12 h;
at t=12-19 h it was constant; and after t=19 h pH increased.
10. At all the oxygen transfer conditions applied, glucose concentration
(CG0 = 7.0 kg m-3), decreased with the cultivation time, as expected.
At the end of the bioprocess, the lowest amount of glucose was
attained at LimOT and MOT1 conditions that correspond to the
consumption of %91.5 of the initial glucose.
11. At all the conditions, cell concentration increased at a high rate
between t=2-7 h, and then reached the stationary phase. The
highest cell concentrations were obtained at MOT2 and HOT2
conditions as CX= 0.67 kg m-3 and the lowest cell concentration was
obtained at LimOT and HOT1 as CX= 0.54 kg m-3.
12. Because of the inappropriate oxygen transfer the lowest β-
lactamase activity was obtained at LimOT condition where the
lowest cell concentration was obtained. At MOT1 condition β-
lactamase activity was higher than the other conditions throughout
the process but at t=24 h LOT2 and MOT1 gave all most the same β-
lactamase activity values ca. A=90 U cm-3. In the process the
cultivation time in which the highest β-lactamase activity was
98
obtained shifted 1.33-fold to an earlier cultivation time (t=24h)
compared to the laboratory scale experiments (t=32h) with a cost
of 22 % lower activity.
13. In general the amino acid concentrations in the fermentation broth
was low and considering all the amino acid profiles and oxygen
transfer conditions, arginine concentration was the highest at LimOT
condition obtained as 0.072 kg m-3 at t=3 h. At all the oxygen
transfer conditions, generally aspartic acid and the asparagine were
the amino acids detected in the broth. The total amino acid
concentration excreted to the fermentation broth was maximum at
LOT2 condition at t=24 h as TOA = 0.133 kg m-3 and minimum at
HOT1 condition at t=20 h as TOA = 0.001 kg m-3.
14. At all the oxygen transfer conditions, acetic acid and lactic acid are
the organic acids detected in the broth at high concentrations. At
LimOT condition at t=11 h lactic acid was excreted having the
concentration of 1.464 kg m-3 which was the highest value obtained
throughout the bioprocess. Moreover, the total organic acid
concentration excreted to the fermentation broth was maximum at
LimOT condition at t=20 h as TOA = 2.513 kg m-3, explaining the
reason of the highest rate of decrease in the medium pH at this
condition. Under the lower range of oxygen transfer conditions,
LimOT and LOT1, due to the insufficient operation of TCA cycle α-
ketoglutaric and succinic acid were excreted to the fermentation
broth.
15. Average KLa, increased with the increase in the agitation and
aeration rates and its values varied between 0.007-0.044 s-1. There
is a fairly good agreement between the experimental and correlated
values for coelescing bubbles (Eq 1-4) given by Moo-Young and
Blanch (1981), within the agitation and air-inlet rate range used.
Because of the dynamic behavior of the fermentation media, KLa
could not be correlated for the entire fermentation process.
99
16. In general the enhancement factors E were slightly higher than 1.0,
showing that a slow reaction is accompanied by mass transfer and
they did not show a significant difference at the oxygen transfer
conditions applied and changed in the range between E= 1.0-2.1.
17. LimOT, LOT1 and LOT2 conditions, were the mass-transfer limited
conditions (Da>>1). While, at MOT1, MOT2, HOT1, and HOT2
conditions, at=2-8 h mass-transfer resistance was more effective
(Da>>1).
The high effectiveness factor, η, values until t=5 h indicate that the
cells are consuming oxygen with such a high rate that maximum
possible oxygen utilization (OD) value is approached and thereafter
the decrease in η indicates that the cells are consuming lower
oxygen than the oxygen demand (OD).
18. At all the oxygen transfer conditions applied the specific growth
rates decreased in the logarithmic growth phase and at stationary
phase they reached a constant value µ=0 h-1. The maximum specific
growth rate of µmax=1.04 h-1 was obtained at t=1 h at LOT1
condition.
19. The specific substrate consumption rates first decreased and then
increased all the conditions except, LimOT and HOT1 at which they
gradually decreased throughout the fermentation. The highest value
of qS was obtained at t=2 h of LOT1 condition as 2.17 kg kg-1 h-1;
where the lowest value was obtained at t=28 h of LimOT and HOT1
conditions as 0.07 kg kg-1 h-1.
20. The specific oxygen uptake rates decreased throughout the
bioprocess due to the increased cell concentration and gave a
maximum at LimOT condition at t=2 h as q0=0.94 kg kg-1 h-1 and a
minimum at LOT1 condition at t=28 h as q0=0.08 kg kg-1 h-1.
21. In the β-lactamase formation the specific production rate decreased
throughout the process at all the oxygen transfer conditions applied
but at LimOT and LOT1 conditions after t=20 h the specific
100
production rate again began to increase. The highest value of qp
was obtained at t=0.5 h at LOT2 condition as 69.5*106 U kg-1h-1.
22. The yield of cell on substrate and the yield of cell on oxygen
decreased with the cultivation time at all the oxygen transfer
conditions applied however at LimOT condition they increased
between t=2-5 h. The highest YX/S value was obtained at MOT1
condition at t=2 h as YX/S=0.72 kg kg-1 and the yield of cell on
oxygen reached a maximum, YX/O=1.49 kg kg-1, at t=2 h at MOT1
condition. The yield of substrate on oxygen showed a decrease
and/or an increase throughout the fermentation and gave the
highest value at HOT2 condition at t=20 h as YS/O=8.07 kg kg-1.
Moreover at HOT2 condition the YS/O values increased with the
cultivation time after t=5 h, indicating the increase in the efficiency
of energy metabolism.
23. Because product and by-product formations in the bioprocess for β-
lactamase production are dependent on the oxygen transfer rate,
well-defined perturbations were achieved by the four different
oxygen transfer conditions., i.e., limited-, low-, medium-, and high-
oxygen transfer rates, and an in-depth insight was provided by
applying metabolic flux analysis. The change in the oxygen transfer
rate influenced the fluxes of the central pathways and consequently,
the formation of the key intermediates including the amino acids,
and consequently β-lactamase production throughout the
bioprocess.
24. The only carbon source in the defined medium was glucose that
enters into the carbon mechanism in the glycolysis pathway. The
fluxes through glycolysis pathway were active at all the oxygen
transfer conditions. However, in period I at LimOT and LOT1 and in
period III at MOT1 conditions; and in period III at LOT1 and in period
I at MOT1 conditions the Pyr formation reaction (R14), and in period
II at MOT1 the AcCoA formation reaction (R16) from Pyr and in
period III at LimOT, in period II and IV at LOT1 condition, in period
IV at MOT1 and in period III at HOT2 conditions both R14 and R16
were inactive in the glycolysis pathway. Moreover, the
101
gluconeogenesis pathway reactions were inactive at all the
conditions.
25. The key intermediate R5P formation was achieved by branching at
F6P through the interconversion reactions since the fluxes from G6P
to both Glc (R2) and Gluc6P (R17) were inactive in period I at
LimOT, in period IV at LOT1, in period II and IV at MOT1 and in
period III at HOT2 conditions. Nevertheless, in period III at LimOT,
in period I, II and III at LOT1, in period I and III at MOT1 and in
period I at HOT2 conditions R5P was produced using the oxidative
reaction.
26. Because NADH and FADH2 are generated in the TCA cycle and
transfer their electrons to the molecular oxygen during the ATP
generation by the oxidative phosphorylation and are then
regenerated in the TCA cycle, the rate of the TCA cycle was strongly
dependent on the oxygen transfer conditions. The successful
operation of TCA cycle was observed in period III at LimOT and
LOT1 conditions and in period IV at MOT1 conditons. The flux of the
anaplerotic reaction either R35 or R36 that connects the TCA cycle
respectively, from either Mal or OA to the gluconeogenesis pathway
via Pyr was influenced by the oxygen transfer rate. In Period II at
LimOT condition Pyr was produced by the reaction R36.
Nevertheless, in period II at LOT1 and MOT1 conditions, the
connection of the TCA cycle to Pyr was achieved via OA through the
reaction R35.
27. The total ATP generation was the highest in period IV at MOT1
condition, while the ATP requirements for the transport,
translocation, and maintenance of the gradients stated in the model
as the hydrolysis of ATP (R147), was the highest at LOT1 condition.
28. The maximum β-lactamase concentration and activity were obtained
experimentally at MOT1 condition; however the metabolic flux
analysis showed that the β-lactamase synthesis flux (R149) was the
highest in Period I at HOT2 condition, in period II at LOT1 condition
and in period IV of MOT1 condition. Amongst the highest β-
lactamase flux was obtained in period IV at MOT1 condition. On the
102
bases of the results the following oxygen transfer strategy can be
proposed:
In the bioreactor based on the periods of the bioprocess for the
exponentional growth phase the high-oxygen transfer, for the
stationary phase low–oxygen transfer, and for the β-lactamase
synthesis period the medium-oxygen transfer conditions can be
applied to fine tune bioreactor performance.
103
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109
APPENDIX A
Calibration of Bacillus licheniformis Concentration
0.0
0.1
0.1
0.2
0.2
0.3
0.3
0.4
0.4
0.5
0.0 0.2 0.4 0.6 0.8 1.0 1.2
Cx, kg m-3
Abso
rbance
Figure A.1 Calibration curve for Bacillus licheniformis concentration
Slope of the calibration curve, m=2.49 1/kg m-3 (λ=600 nm)
tioDilutionRaAbsorbanceCx ×=49.2
110
APPENDIX B
Calibration of Beta-Lactamase Activity
y = 1.836xR2 = 0.9993
y = 0.688xR2 = 0.9998
0.0
0.2
0.4
0.6
0.8
1.0
1.2
1.4
0.0 0.2 0.4 0.6 0.8
Cbenzylpenicillin, Cpenicilloic acid (mM)
Abso
rban
ce
Figure A.2 Calibration Curve of the benzylpenicillin and penicilloic acid in 0.1 M phosphate buffer, pH=7.0, T=30°C, λ=232nm. Benzylpenicillin, (♦); Penicilloic acid, (▲).
One unit of β-lactamase activity was defined as the amount of enzyme that
could hydrolyze 1µmol of benzylpenicillin at 30°C and pH 7.0 in one minute. The
product of the hydrolysis reaction, penicilloic acid, also gives an absorbance at
232nm, therefore, the difference of the slopes is taken, m1-m2=1.148 mM-1. The
activity, U cm-3 is given by (Çelik, 2003),
atioxDilutionRcmlx
mmolUx
mMmmAmC
A A3331
21
10
101
101
)( −−−−
= λ
111
APPENDIX C
Calibration of Beta-Lactamase Concentration
y = 55432x
0
2000
4000
6000
8000
10000
12000
0.0 0.1 0.2 0.3 0.4 0.5 0.6
CB, kg m-3
Are
a
Figure C.1 Calibration curve for beta-lactamase concentration
tioDilutionRaAreaCB ×=55432
112
APPENDIX D
Calibration of Serine Alkaline Protease Concentration
y = 159690x
0
2000
4000
6000
8000
10000
12000
14000
16000
18000
0.0 0.1 0.2 0.3 0.4 0.5 0.6
CSA P , kg m-3
Are
a
Figure D.1 Calibration curve for serine alkaline protease concentration
tioDilutionRaAreaCSAP ×=159690
113
APPENDIX E
Calibration of Reduced Sugar Concentration
0.0
0.1
0.2
0.3
0.4
0.5
0.6
0.7
0.8
0.9
0.0 0.1 0.2 0.3 0.4
CG , kg m-3
Abso
rban
ce
Figure E.3 Calibration Curve of the DNS solution
tioDilutionRaAbsorbanceCG ×
+
=938.3
3394.0
y=3.938x-0.3394
114
APPENDIX F
Preparation of DNS Solution
1. a) 880 cm3 of 1 % (m/v) DNS solution is prepared by dissolving 8.8 g
dinitrosalisilyc acid in 880 cm3 distilled water.
b) After addition of 225 g ROCHELLE salt (sodium potassium tartarate),
the solution is mixed.
c) 300 cm3 of 4.5 % NaOH, prepared by dissolving 13.5 g NaOH in 300
cm3 distilled water, is added to this solution.
2. a) 22 cm3 10 % NaOH, is prepared by dissolving 2.2 g NaOH in 22 cm3
distilled water.
b) 10 g christalized phenol and 100 cm3 distilled water are added to the
solution.
c) 60 cm3 is taken from this alkali-phenol mixture, 6.9 g NaHCO3 is added
and mixed.
The solution obtained from the first step is mixed with that from the second
step and then they are stirred until ROCHELLE salt is dissolved. The
prepared solution is kept in dark-colored bottle at 4°C and it should be used
after 48 h.
115
APPENDIX G
Metabolic Reactions for Bacillus licheniformis
Glycolysis and Gluconeogenesis Pathway
1. Glc + PEP → G6P + Pyr
2. G6P → Glc + Pi
3. F6P → G6P
4. G6P → F6P
5. Frc + PEP → F6P + Pyr
6. Man + PEP → Man6P + Pyr
7. Man6P → F6P
8. F6P + ATP → 2T3P + ADP
9. 2T3P → F6P + Pi
10. T3P + ADP + Pi → PG3 + ATP + NADH
11. PG3 + ATP + NADH → T3P + ADP + Pi
12. PG3 → PEP
13. PEP → PG3
14. PEP + ADP → Pyr + ATP
15. Pyr + 2ATP → PEP + 2ADP
16. Pyr → AcCoA + CO2 + NADH
Pentose Phosphate Pathway
17. G6P → Gluc6P + NADPH
18. Glc → Gluc + NADH
19. Gluc + ATP → Gluc6P + ADP
20. Gluc6P → R5P + CO2 + NADPH
21. R5P → Xyl5P
22. Xyl5P → R5P
23. R5P → Rib5P
24. Rib5P → R5P
25. Xyl5P + Rib5P → S7P + T3P
26. S7P + T3P → Xyl5P + Rib5P
27. Xyl5P + E4P → F6P + T3P
116
28. F6P + T3P → Xyl5P + E4P
29. T3P + S7P → F6P + E4P
30. F6P + E4P → T3P + S7P
Branches from Glycolysis
31. Pyr + NADH → Lac
32. Lac → Pyr + NADH
33. AcCoA + ADP + Pi → Ac + ATP
34. Ac + ATP → AcCoA + ADP + Pi
Anapleoric Reactions
35. Mal → Pyr + CO2 + NADPH
36. OA → Pyr + CO2
TCA Cycle
37. AcCoA + OA → Cit
38. Cit → ICit
39. ICit → αKG + CO2 + NADPH
40. αKG → SucCoA + CO2 + NADH
41. SucCoA + Pi + ADP → Suc + ATP + CoA
42. Suc + ATP → SucCoA + ADP + Pi
43. Suc → Fum + FADH2
44. Fum → Mal
45. Mal → OA + NADH
46. ICit → Glx + Suc
47. Glx + AcCoA → Mal
Biosynthesis of Serine Family Amino Acids
48. PG3 + Glu → Ser + αKG + NADH + Pi
49. Ser + THF → Gly + MetTHF
50. Ser + AcCoA + H2S → Cys + Ac
Biosynthesis of Alanine Family Amino Acids
51. Pyr + Glu → Ala + αKG
52. 2Pyr + NADPH → KVal
53. KVal + Glu → Val + αKG
54. KVal + AcCoA + Glu → Leu + αKG + NADH + CO2
117
Biosynthesis of Histidine
55. R5P + ATP → PRPP + AMP
56. PRPP + ATP + Gln → His + PRAIC + αKG + 2PPi + 2NADH + Pi
Biosynthesis of Aspartic Acid Family Amino Acids
57. OA + Glu → Asp + αKG
58. Asp + Gln + ATP → Asn + Glu + AMP + PPi
59. Asp + ATP + NADPH → AspSa + ADP + Pi
60. AspSa + Pyr → DC
61. DC + NADPH → Tet
62. Tet + AcCoA + Glu → Ac + αKG + mDAP
63. mDAP → Lys + CO2
64. AspSa + NADPH → HSer
65. HSer + ATP → Thr + ADP + Pi
66. Thr + Pyr + NADPH + Glu → Ile + αKG + NH3 + CO2
67. AcCoA + Cys + HSer + H2S + MTHF → Met + Pyr + 2Ac + NH3 + THF
Biosynthesis of Aromatic Amino Acids
68. 2PEP + E4P + ATP + NADPH → Chor + ADP + 4Pi
69. Chor + Glu → Phe + αKG + CO2
70. Chor + Glu → Tyr + αKG + NADH + CO2
71. Chor + NH3 + PRPP → Pyr + IGP + CO2 + PPi
72. IGP + Ser → Trp + T3P
Biosynthesis of Glutamic Acid Family Amino Acids
73. αKG + NH3 + NADPH → Glu
74. Glu + ATP + NH3 → Gln + ADP + Pi
75. Glu + ATP + 2 NADPH → Pro + ADP + Pi
76. 2Glu + AcCoA + ATP + NADPH → Orn + αKG + Ac + ADP + Pi
77. Orn + CaP → Citr + Pi
78. Citr + Asp + ATP → Arg + Fum + AMP + PPi
Catabolism of the amino acids
79. αKG + Ala → Pyr + Glu
80. Arg + αKG → 2Glu + NH3 + NADPH + CO2
81. Asn → Asp + NH3
82. Asp → Fum + NH3
118
83. Cys → Pyr + NH3 + H2S
84. Gln + αKG + NADPH → 2Glu
85. Gly + MetTHF → Ser + THF
86. His + THF → Glu + MeTHF
87. Ile + αKG → Glu + FADH2 + 2NADH + CO2 + SucCoA + AcCoA
88. Leu + αKG + ATP → Glu + FADH2 + NADH + 2AcCoA + ADP + Pi
89. Phe → Tyr + NADPH
90. Pro → Glu + NADPH
91. Ser → Pyr + NH3
92. Thr → Gly + NADH + AcCoA
93. Trp + NADPH → AcCoA + Ala
94. Tyr + αKG + SucCoA → Glu + Fum + AcCoA + Succ + CO2
95. Val + αKG → Glu + FADH2 + 3NADH + 2CO2 + SucCoA
Biosynthesis of Nucleotides
96. PRPP + 2Gln + Asp + 2H2O + CO2 + Gly + 4ATP + F10THF →
2Glu + PPi + 4ADP + 4Pi + THF + PRAIC + Fum
97. PRAIC + F10THF → IMP + THF
98. IMP + Gln + ATP → NADH + GMP + Glu + AMP + PPi
99. GMP + ATP → GDP + ADP
100. ATP + GDP → ADP + GTP
101. GTP + ADP → ATP + GDP
102. NADPH + ATP → dATP
103. NADPH + GDP + ATP → ADP + dGTP
104. IMP + GTP + Asp → GDP + Pi + Fum + AMP
105. AMP + ATP → 2ADP
106. PRPP + Asp + CaP → UMP + NADH + PPi + Pi + CO2
107. UMP + ATP → UDP + ADP
108. UDP + ATP → ADP + UTP
109. UTP + NH3 + ATP → CTP + ADP + Pi
110. ATP + NADPH + CDP → dCTP + ADP
111. CDP + ATP → CTP + ADP
112. CTP + ADP → CDP + ATP
113. UDP + MetTHF + 2ATP + NADPH → dTTP + DHF + 2ADP + PPi
Biosynthesis and interconversion of one-carbon units
114. DHF + NADPH → THF
119
115. MetTHF + CO2 + NH3 + NADH → Gly + THF
116. MetTHF + NADPH → MTHF
117. MetTHF → MeTHF + NADPH
118. MeTHF → F10THF
119. Gly + THF → MetTHF + NH3 + NADH + CO2
Transhydrogenation reaction
120. NADH → NADPH
121. NADPH → NADH
Electron Transprt System (P/O=2)
122. NADH + 2ADP + 2Pi → 2ATP
123. FADH2 + ADP + Pi → ATP
Transport Reactions
124. CO2 → exp
125. imp → CO2
126. imp → NH3
127. NH3 → exp
128. 2ATP + 4 NADPH → AMP + ADP + H2S + PPi + Pi
129. PPi → 2Pi
130. imp → Pi
131. Pi → exp
Biosynthesis of Fatty Acids
132. T3P + NADPH → GL3P
133. 7AcCoA + 6ATP + 12NADPH → C14:0 + 6ADP + 6Pi
134. 7AcCoA + 6ATP + 11NADPH → C14:1 + 6ADP + 6Pi
135. 8.2AcCoA + 7.2ATP + 14 NADPH → 7.2PI + 7.2ADP + PA
136. 2ATP + CO2 + Gln → CaP + Glu + 2ADP + Pi
Other Biomass Components
137. F6P + Gln + AcCoA + UTP → UDPNAG + Glu + Ppi
138. PEP + NADPH + UGPNAG → UDPNAM + Pi
139. R5P + PEP + CTP → CMPKDO + PPi + 2Pi
140. Ser + CTP + ATP → CDPEtN + ADP + PPi + CO2
141. S7P + ATP → ADPHep + PPi
142. G6P → G1P
120
143. G1P → G6P
144. UTP + G1P → UDPGlc + PPi
Biomass Synthesis
145. 0.5352Ala + 0.28Arg + 0.22Asn + 0.22Asp + 0.09Cys + 0.09His +
0.25Gln + 0.25Glu + 0.58Gly + 0.27Ile + 0.42Leu + 0.32Lys + 0.14Met +
0.0593Orn + 0.17Phe + 0.2Pro + 0.377Ser + 0.05Trp + 0.13Tyr + 0.24Thr
+ 0.4Val + 0.2GTP + 0.13UTP + 0.12CTP + 0.22DATP + 0.02DCTP +
0.02DGTP + 0.02DTTP + 0.129GL3P + 0.0235C140 + 0.0235C141 +
0.259PA + 0.0433UDPNAG + 0.0276UDPNAM + 0.0235CMPKDO +
0.0235CDPETN + 0.0157UDPGLC + 0.02354ADPHEP + 0.154G1P +
41.139ATP → Biomass + 41.139ADP + 41.139Pi
Serine Alkaline Protease Synthesis
146. (0.145Ala + 0.0146Arg + 0.0657Asn + 0.0328Asp + 0.0255Gln +
0.0182Glu + 0.127Gly + 0.0182His + 0.0365Ile + 0.0584Leu + 0.0328Lys +
0.0182Met + 0.0146Phe + 0.0365Pro + 0.116Ser + 0.0729Thr + 0.0036Trp
+ 0.0474Tyr + 0.113Val) x 274 + 5.5ATP → SAP + 5.5ADP + 5.5Pi
Maintenance
147. ATP → ADP + Pi
148. Pyr + CO2 → OA
β-Lactamase Synthesis
149. 24Ala + 14Arg + 13Asn + 23Asp + 8Gln + 21Glu + 16Gly + 1His + 14Ile
+ 27Leu + 24Lys + 4Met + 7Phe + 11Pro + 11Ser + 23Thr + 3Trp + 6Tyr +
15Val + 5.5ATP → β-lactamase + 5.5ADP + 5.5Pi
![Chapter 10: Sterilization and Bioreactor Operationpages.mtu.edu/~drshonna/cm4710f07/lectures/chapter10.pdf · Chapter 10: Sterilization and Bioreactor Operation ... [N(t)]= expected](https://img.pdfslide.us/doc/110x75/5aa40f1f7f8b9ac8748b646d/chapter-10-sterilization-and-bioreactor-drshonnacm4710f07lectureschapter10pdfchapter.jpg)
